Process for the hydroxylation of olefins using molecular oxygen, an osmium containing catalyst, a copper Co-catalyst, and an aromatic amine based promoter

ABSTRACT

A process directed to the hydroxylation of olefins by reacting said olefins in the presence of oxygen, water, and a catalyst composition comprising (i) a catalytically active osmium containing compound, (ii) a Co-catalyst I comprising a copper containing compound such as CuBr 2 , and (iii) a Co-catalyst II capable of increasing the rate and/or selectivity of the hydroxylation reaction, such as pyridine is disclosed.

BACKGROUND OF THE INVENTION

The present invention relates to a process for converting olefinically unsaturated compounds directly to their corresponding diols or polyols in the presence of a specifically defined oxidation catalyst composition, water, and an oxygen containing gas.

It is well known from the technical literature, that olefins can be oxidized to their corresponding diols, stoichiometrically or catalytically with osmium oxide compounds, particularly osmium tetroxide.

The non-catalytic, i.e. stoichiometric, cis-hydroxylation of alkenes with OsO₄ has been conventionally characterized as taking place via the formation, with the alkene, of an osmium (VI) intermediate ester complex. (For a recent review, see, "Osmium Tetroxide Cis Hydroxylation of Unsaturated Substrates", by M. Schroder, Chem. Rev. Vol 80, pp. 187-213 (1980) hereinafter Schroder).

To convert the non-catalytically prepared osmium (VI) ester complex intermediate to the diol, the intermediate can be hydrolyzed reductively. Reductive hydrolysis is conventionally carried out by using alkali metal sulfites, bisulfites, lithium aluminum hydride, or hydrogen sulfide to yield the corresponding cis-diols together with lower valence forms of osmium which are removed by filtration.

It has been observed by Criegee (see Schroder, page 191, Col. 1 11-12) that for non-catalytic cis hydroxylation of alkenes, the rate of formation of the Osmium (VI) ester complex is greatly increased in the presence of tertiary amines such as pyridine. This rate enhancement is believed to occur via the formation of some type of amine Osmium (VI) ester complex (see Schroder page 191, Col. 2). However, enhancement of the rate of the Osmium (VI) ester complex does not necessarily result in an enhancement of the overall hydroxylation rate, since the rate of hydrolysis of the ester complex must also be considered. In this regard, it has been noted that whereas certain osmium ester complexes and amine ester complexes (e.g. with pyridine) can be hydrolyzed reductively, amine ester complexes are more resistant to such hydrolysis. (See Schroder page 191, Col. 2, last paragraph; and page 193, Col. 1, first paragraph).

In contrast to the stoichiometric non-catalytic mode of cis hydroxylation with OsO₄, the catalytic mode employs a secondary oxidant to oxidatively hydrolyze the intermediate Osmium (VI) ester and regenerate the OsO₄ which can undergo further reduction by the substrate olefin. A variety of oxidants have been employed in conjunction with OsO₄ such as H₂ O₂, t-butylhydroperoxide and oxygen.

The use of oxygen as an oxidant has encountered considerable difficulty due to the appreciable overoxidation of the products, particularly at elevated temperatures (e.g. 70°-80° C.), leading to the formation of keto or acid products. However, if the reaction temperature is lowered to reduce overoxidation, the reaction rate is so low that yields of cis-diol are drastically reduced. An additional disadvantage of the use of oxygen oxidant is that the reaction is highly pH dependent (see Schroder, page 210, Col. 1).

The poor performance of oxygen based osmium catalyzed olefin hydroxylation systems is unfortunate, since such systems have inherent advantages over organic hydroperoxide based systems. For example, hydroxylation systems employing organohydroperoxide oxidants result in the conversion of the organohydroperoxide to its corresponding alcohol during the formation of the desired olefin derived diol. Thus, for example, t-butylhydroperoxide is converted to t-butylalcohol. The commercial attractiveness of such processes is dependent on the ability to use or sell the organic alcohol co-product in addition to the diol. Given the fluctuation in economic conditions, however, it may be difficult to dispose of large quantities of these organic alcohol co-products in an economically attractive manner. In any event, it can be troublesome, when the quantity of one product, selected on the basis of marketing possibilities for a given period, necessarily determines the quantity of some other product which may be smaller or larger than desirable in view of changing marketing requirements within that same period. It can, therefore, under certain circumstances be considered as a disadvantage of the aforenoted organohydroperoxide based processes that such large quantities of organic alcohols are formed as co-products, even though under other circumstances the formation of two products may well be found acceptable.

In contrast, oxygen based hydroxylation systems do not produce an oxidant derived alcohol co-product that must be disposed of, which can be a significant advantage.

The search has, therefore, continued for ways of improving the rate and/or selectivity of osmium catalyzed oxygen based processes for hydroxylating olefins.

One step in this direction, is disclosed in commonly assigned U.S. Pat. No. 4,390,739 by R. Austin and R. Michaelson. This patent describes a process for the hydroxylation of olefins using oxygen as an oxidant, a catalytically active metal oxide catalyst such as OsO₄, and at least one transition metal salt co-catalyst such as copper bromide. This process can also be conducted in the optional presence of a second co-catalyst such as alkali metal halides. Pyridine is disclosed as a suitable solvent for this process but no mention is made of any promoting effect being associated with this solvent medium. While the use of the transition metal co-catalyst substantially improves the reaction rate and/or selectivity of the hydroxylation reaction, a further improvement in this process is still being sought.

U.S. patent application Ser. No. 310,217, filed Oct. 9, 1981, now abandoned, of common assignee herein by R. Michaelson and R. Austin discloses the use of various osmium halide and oxyhalide catalysts in the presence or absence of a wide variety of co-catalysts and an oxidant selected from hydrogen peroxide, organohydroperoxides, or oxygen. Pyridine is disclosed as a suitable buffer for pH control in this application, which pH control is required when employing hydrogen peroxide.

Commonly assigned U.S. Pat. No. 4,314,088 and a continuation-in-part thereof, namely, U.S. Pat. No. 4,393,253 by R. Austin and R. Michaelson collectively, disclose the use of various halide containing co-catalysts in conjunction with osmium tetroxide catalyst and organohydroperoxide oxidants to hydroxylate olefins. The halide containing co-catalysts include alkali and alkaline earth metal halides, hydrogenhalides, quaternary hydrocarbyl phosphonium halides, halogens, and transition metal halides.

U.S. patent application Ser. No. 399,270 filed July 19, 1982, by R. Austin and R. Michaelson is directed to a process for hydroxylating olefins in the presence of an organohydroperoxide oxidant, an osmium containing catalyst and an organic halogenated hydrocarbon co-catalyst.

Commonly assigned U.S. patent application Ser. No. 394,414, filed July 1, 1982 by R. Michaelson and R. Austin, is directed to the use of carboxylate salts as co-catalysts for use in conjunction with osmium oxides as a catalyst and organohydroperoxide as oxidant to hydroxylate olefins.

Commonly assigned allowed U.S. patent application Ser. No. 397,997 filed July 14, 1982, now U.S. Pat. No. 4,413,151, by R. Michaelson, R. Austin, and D. White is directed to a process for hydroxylating olefins in the presence of a supported osmium containing catalyst, optional co-catalysts (e.g. CuBr₃) and an oxidant selected from hydrogen peroxide, organohydroperoxides and oxygen.

Commonly assigned U.S. patent application Ser. No. 420,137 filed Sept. 20, 1982 by R. Michaelson, R. Austin and D. White is directed to a process for hydroxylating olefins in the presence of an osmium carbonyl catalyst optional co-catalysts and an oxidant selected from hydrogen peroxide, organohydroperoxide, and oxygen.

Commonly assigned U.S. patent application Ser. No. 440,964, filed Nov. 12, 1982 by R. Michaelson, R. Austin, and D. White is directed to a process for hydroxylating olefins in the presence of an osmium oxide catalyst, optional co-catalysts and sodium hydroxide as a promoter.

While all of the above described commonly assigned patents or patent applications disclose the use of pyridine as one of many suitable solvents, none of these applications show or suggest either alone or collectively, that any promoting effect can be obtained from pyridine when employed in accordance with the presently claimed invention.

Moreover, to the best of the inventors' knowledge, not a single prior art publication shows the use of any tertiary amine as a promoter to enhance the overall rate of osmium catalyzed cis-hydroxylation of olefins with oxygen. While catalytic cis-hydroxylation of tetra and tri-substituted alkenes with t-butylhydroperoxide and OsO₄ has apparently been conducted in the presence of pyridine, the oxidative hydrolysis of such esters has been found to be particularly slow due to steric considerations (see, Schroder, page 193, Col. 2, first paragraph).

Notwithstanding the above, the following discussion is intended to provide a background of osmium based olefin hydroxylation processes.

U.S. Pat. No. 3,335,174, is directed to the use of Group Vb, VI-b and VII metal halides and oxyhalides (e.g., OsCl₃) as hydroxylation and esterification catalysts in conjunction with aqueous H₂ O₂ as an oxidant. However, the process for using this catalyst requires the presence of lower aliphatic hydrocarbon acids such as glacial, formic, acetic and propionic acid as solvents. Under these conditions the reaction times vary from 1/2 to 4 hours, but at the shorter reaction times it is disclosed that substantial amounts of epoxide result thereby indicating that the reaction proceeds via the peracid route. The only yield disclosed is obtained in connection with tungsten hexachloride in Example 1. This yield is extremely low, i.e. 22%, and includes both half-acetate and diol. When an equivalent of Example 2 of this patent was conducted, the conversion of hydrogen peroxide was found to be 10%, the selectivity to diol was 10%, the selectivity to diacetate was 20% and the diol yield was 1%. Thus, among the major disadvantages of the process described in this patent are the low selectivities to diol and the corrosiveness of metal halides in the presence of glacial acids such as acetic acid.

Japanese Patent Application No. Sho 54-145604, published Nov. 14, 1979, is directed to a process for hydroxylating olefins in the presence of OsO₄, a quaternary ammonium salt such as tetraethylammonium bromide, and a peroxide including organoperoxides and H₂ O₂ as the oxidant. The use of oxygen as the oxidant is not disclosed nor is the co-presence of co-catalyst I salts as described herein disclosed. Selectivities to glycol of from about 4.5 to about 66% are disclosed. H₂ O₂ oxidant in combination with OsO₄ is known as Milas reagent which can lead to non-selective oxidation of olefins as well as over oxidation. H₂ O₂ is also substantially more expensive than oxygen or air. Accordingly, the uses of organohydroperoxides as well as H₂ O₂ as oxidants are each associated with their own disadvantages.

U.S. Pat. No. 2,214,385 discloses the use of hydrogen peroxide and a catalytically active oxide, such as osmium tetroxide, dissolved in an essentially anhydrous, non-alkaline, inert, preferably organic, solvent, to convert, by oxidation, unsaturated organic compounds to useful oxygenated products such as glycols, phenols, aldehydes, ketones, quinones and organic acids. The formation of glycols is achieved by conducting the reaction at temperatures of between several degrees below 0° C. and 21° C. Such low reaction temperatures drastically and disadvantageously, reduce the reaction rate to commercially unacceptable levels. At temperatures greater than 21° C., the formation of aldehydes, ketones, and acids is favored.

U.S. Pat. No. 2,773,101 discloses a method for recovering an osmium containing catalyst such as osmium tetroxide, by converting it to the non-volatile osmium dioxide form, distilling the hydroxylation product, reoxidizing the osmium dioxide to the volatile osmium tetroxide, and then recovering the same by distillation. Suitable oxidizing agents used to re-oxidize the osmium dioxide, include inorganic peroxides such as hydrogen peroxide, sodium peroxide, barium peroxide; organic peroxides, such as t-butyl peroxide or hydroperoxide, benzoyl peroxide; as well as other well known oxidizing agents such as oxygen, perchlorates, nitric acid, chlorine water and the like. As with other methods of the prior art, the above process yields undesirable by-products (see Col. 1, line 55) thus reducing the selectivity of the process.

British Patent Specification No. 1,028,940 is directed to a process for regenerating osmium tetroxide from reduced osmium oxides by treatment of the latter with molecular oxygen in an aqueous alkaline solution. More specifically, it is disclosed that when osmium tetroxide is used by itself as an oxidizing agent, or as a catalyst in conjunction with other oxidizing agents, to oxidize hydrocarbons the osmium tetroxide becomes reduced, and in its reduced form is less active than osmium tetroxide itself. Consequently, by conducting the oxidation reaction in the presence of an alkaline medium and supplying oxygen to the medium throughout the process, the osmium tetroxide is maintained in a high state of activity. The oxidation products disclosed include not only ethylene glycol from ethylene but also organic acids from such compounds as vicinal glycols, olefins, ketones, and alcohols. While the pH of the alkaline medium is disclosed broadly for all possible reactions as varying from 7.5 to 12 for purposes of re-oxidizing reduced osmium tetroxide, the pH employed in the example for preparing ethylene glycol is 9.5. If the pH is too high, a wide variety of products are produced as a result of over oxidation and/or degradation. Thus, the sensitivity of the process to the pH of the medium necessitates rigid pH control which is economically disadvantageous.

U.S. Pat. No. 4,255,596 is directed to a process for preparing ethylene glycol in a homogeneous single-phase reaction medium using ethylbenzene hydroperoxide as the oxidizing agent dissolved in ethylbenzene and osmium tetroxide as the catalyst. The pH of the reaction medium is maintained at about 14 by the presence of tetraalkyl ammonium hydroxide. A small amount of water can dissolve beneficially in the medium to reduce by-product formation and improve selectivity to the glycol.

U.S. Pat. No. 4,049,724 describes the preparation of glycols from alkenes and from unsaturated alcohols in an aqueous system using osmium tetroxide and specifying stable and water-soluble aliphatic hydroperoxides, such as tert-butyl hydroperoxide, while a critical pH of 8 to 12 is maintained by a suitable combination of alkali metal buffering compounds. The preparation of propylene glycol utilizing tert-butyl hydroperoxide is exemplified in the patent at a selectivity based on the hydroperoxide of 45 percent.

None of the aforenoted patents disclose the osmium containing-co-catalytic system described herein.

See also: U.S. Pat. No. 3,317,592 (production of acids and glycols using oxygen as oxidant, OsO₄ as catalyst at pH 8-10); U.S. Pat. No. 3,488,394 (discloses hydroxylation of olefins by reacting olefin and hypochlorite in the presence of OsO₄); U.S. Pat. No. 3,486,478 (discloses reaction of hypochlorite and olefin in an aqueous medium and in the presence of OsO₄ catalyst to hydroxylate the olefin); U.S. Pat. No. 3,928,473 (hydroxylation of olefins to glycols with O₂ oxidant, octavalent osmium catalyst (e.g., OsO₄), and borates as promoter); U.S. Pat. No. 3,931,342 (discloses a process for recovering glycols from an aqueous solution containing alkali metal borate and osmium compounds (e.g., OsO₄); U.S. Pat. No. 3,953,305 (discloses use of OsO₄ catalyst for hydroxylating olefins which is regenerated by oxidizing hexavalent osmium with hexavalent chromium and electrochemically regenerating hexavalent chromium); U.S. Pat. No. 4,203,926 (discloses ethylbenzene hydroperoxide as oxidant used in two phase system to hydroxylate olefins in presence of OsO₄ and cesium, rubidium and potassium hydroxides); U.S. Pat. No. 4,217,291 (discloses the oxidation of Osmium (III) or (IV) in an ionic complex with oxygen and an alkali metal, ammonium, or tetra (-lower) alkyl ammonium cation to a valency of greater than +5+organo hydroperoxides); and U.S. Pat. No. 4,229,601 (discloses the use of cesium, rubidium and potassium hydroxides as promoters for OsO₄ catalyst and t-butyl hydroperoxide oxidant for hydroxylating olefins).

SUMMARY OF THE INVENTION

The present invention resides in the discovery that certain heteroaromatic and/or pseudo heteroaromatic nitrogen containing compounds referred to herein as cocatalyst II can substantially improve the rate of the direct hydroxylation of olefins to their corresponding diols, e.g. vicinal diols, in a reaction system which employs (a) an osmium compound as a catalyst rather than as a stoichiometric oxidant, (b) a transition metal (i.e. copper) containing compound as a co-catalyst, and (c) molecular oxygen as the oxidant to induce oxidative hydrolysis of an osmium-olefin cis-ester intermediate. The present invention represents an improvement over the processes described in commonly assigned U.S. Pat. No. 4,390,739 and U.S. patent application Ser. No. 310,217, filed Oct. 9, 1981, by R. Austin and R. Michaelson.

The direct hydroxylation route of the present invention avoids the formation of an oxirane intermediate that must be hydrolyzed to form the corresponding diol and which can lead to undesirable by-products as is the case of the H₂ O₂ -peracid route to olefin hydroxylation.

Furthermore, the catalytic nature of the present invention is far more cost effective and convenient than osmium stoichiometric routes to olefin hydroxylation.

The accelerating effect of co-catalyst II is quite surprising in the reaction system described herein. For example, in stoichiometric osmium oxide based olefin hydroxylation, one is unconcerned with the reoxidation of stoichiometric osmium oxidant, since once used up it is removed from the reaction system. Consequently, the rate influencing steps in such reactions are the formation of the osmium oxide-olefin cis-ester intermediate and the hydrolysis of the ester. In contrast, in an osmium oxide catalyzed reaction system, the osmium catalyst must go through repeated cycles of reduction and reoxidation. Consequently, the rate of reoxidation of the osmium becomes a significant rate influencing step. Thus, while certain tertiary amines, such as pyridine, are known to accelerate the formation of the cis-ester intermediate in stoichiometric oxidations, it is not known what effect, if any, such amines will have on the overall hydroxylation reaction rate of oxygen based, osmium catalyzed hydroxylations which have been facilitated by a particular transition metal, i.e., copper, co-catalyst. In the environment in which the co-catalyst II rate promoter is employed in the present invention, it has been found that the rate accelerating effect achieved thereby is attributable to interaction with the transition metal of Co-catalyst I rather than with the osmium catalyst. This conclusion is based on the observations, described hereinafter in greater detail, that (1) the promoting effect is a function of the Co-catalyst II/transition metal (i.e., copper) mole ratio, (2) other organic materials conventionally believed to operate as equivalent or better promoters (relative to pyridine) in stoichiometric osmium based hydroxylation reactions, and by similar mechanisms, are inoperative, or in fact operate as rate inhibitors, in the reaction system of the present invention, and (3) the existence of spectral evidence which indicates the presence of a transition metal (i.e., Cu)-pyridine complex in the reaction mixture, the formation of such complexes in general, being well known in the literature. Furthermore, the aforedescribed interaction of copper with Co-catalyst II appears to be unique among the transition metals.

Accordingly, in one aspect of the present invention there is provided a process for hydroxylating at least one olefinic compound having at least one ethylenic unsaturation which comprises reacting said olefinic compound in the presence of oxygen, water, and a catalyst composition in a manner and under conditions sufficient to convert at least one of said ethylenic unsaturation directly to it corresponding diol, said catalyst composition comprising:

(a) at least one catalytically active osmium containing compound;

(b) at least one transition metal containing Co-catalyst I having an identity and in an amount effective to increase at least one of the rate and selectivity of the hydroxylation reaction relative to its absence; said transition metal being copper; and

(c) at least one Co-catalyst II having an identity and in an amount effective to increase the rate of the hydroxylation reaction relative to its absence and represented by the structural formulae (XIa and XIb) hereinafter described.

In another aspect of the present invention the aforedescribed process additionally employs a halo-source to further enhance the rate and/or selectivity of the hydroxylation reaction.

DESCRIPTION OF PREFERRED EMBODIMENTS

In accordance with the present invention, at least one olefin containing at least one ethylenic unsaturation is reacted with oxygen in the presence of water and a catalyst composition comprising a catalytically active osmium containing compound, at least one Co-catalyst I as described herein, at least one Co-catalyst II as described herein, and optionally, but preferably, at least one Co-catalyst III, to convert at least one of said ethylenic unsaturation directly to its corresponding diol.

I. Olefin

Olefins which can be hydroxylated in accordance with the present invention contain at least one ethylenic unsaturation and comprise any of the unsaturated aliphatic or alicyclic compounds well known in the art for undergoing such hydroxylation reactions. Typically, such compounds will contain from 2 to about 20 carbons, preferably from 2 to about 10 carbons, and most preferably from 2 to about 5 carbons. Such compounds may be straight or branched chain, mono-olefinic, di-olefinic, or polyolefinic, conjugated or non-conjugated. There may be substituted with such groups as aryl, preferably aryl of from 6 to about 14 carbons, alkyl, preferably alkyl of from 1 to 10 carbons, or aralkyl and alkaryl wherein the alkyl and aryl portions thereof are as described above, as well as with functional groups such as hydroxyl, carboxyl and anhydride.

Typical of such olefins are those represented by the structural formula: ##STR1## wherein R₁, R₂, R₃, and R₄, which may be the same or different, are selected from the group consisting of hydrogen; substituted or unsubstituted; alkyl, aryl, alkaryl, and aralkyl hydrocarbyl groups, said hydrocarbyl groups being preferably as defined immediately above; or any two or said R₁₋₄ groups together can constitute a cycloalkyl group typically of from about 4 to about 12, preferably from about 5 to about 8 carbons.

Representative olefins which can be hydroxylated and contain at least one ethylenic saturation include: ethylene, propylene, butene-1, butene-2, isobutene, pentene-1, pentene-2, hexene, isohexene, heptene, 3-methylhexene, octene-1, isooctene, nonene, decene, dodecene, tridecene, pentadecene, octadecene, eicosene, docosene, tricosene, tetracosene, pentacosene, butadiene, pentadiene, hexadiene, octadiene, decadiene, tridecadiene, eicosadiene, tetracosadiene, cyclopentene, cyclohexene, cycloheptene, methylcyclohexene, isopropylcyclohexene, butylcyclohexene, octylcyclohexene, dodecylclohexene, acrolein, acrylic acid, 1,2,3,4-tetrahydrophthalic anhydride, allyl alcohol, methyl methacrylate, styrene, cholestrol, and the like.

The preferred olefins are ethylene, propylene, isobutylene, styrene, allyl alcohol and allyl chloride.

The most preferred olefins are propylene, ethylene, and butenes.

II. Osmium Compound (Catalyst)

In accordance with the present invention, it has been found that the oxidation state of osmium in osmium catalyst as initially added to the reaction mixture is not critical to catalytic activity when the appropriate co-catalyst system is employed as described hereinafter, i.e., any osmium compound as described herein when subjected to hydroxylation conditions as described herein, itself possesses, or is converted under such hydroxylation conditions to a species which possesses, the capability of catalyzing the hydroxylation of olefins with oxygen.

In view of the above, it is possible to flexibly tailor the identity of the osmium compound and co-catalyst system described herein to achieve an extremely efficient catalyst system for hydroxylating olefins with oxygen. In selecting the particular osmium compound for use in the present invention, the volatility and/or toxicity of the compound, and its activity in the system employed will be taken into consideration.

More specifically, included within the scope of osmium compound (the term "osmium compound" is defined herein broadly to also include osmium metal as well as ionic and neutral complexes of osmium and a ligand) which can be employed in the process of the present invention include in their order of preference halogenated osmium compounds, ionic osminum compounds, osmium oxides, osmium complexes, osmium carbonyls, and osmium metal.

Representative halogenated osmium compounds are disclosed in U.S. patent application Ser. No. 310,217, filed Oct. 9, 1981 the disclosure of which is herein incorporated by reference.

For example, osmium-halogen containing compounds include osmium halides and osmium oxy halides, and complexes thereof, (all of the above being referred to herein collectively as osmium-halides) such as those represented by the structural formulae: Os(X)_(n) (e.g., OsX₃, OsX₄, and OsX₅); Os(OH)X₃ ; OsOX₄ ; OsO₃ X₂ ; OsONX₄ ; (M)_(n) '[OsX₆ ]⁻² ; (M)_(n) '[OsO₂ X₄ ]⁻² ; M⁺¹ [Os(OH)X₅ ]⁻¹ ; (M)_(n) '[OsO₄ X₂ ]⁻² ; (M)_(n) '[OsO₂ (OH)₂ X₂ ]⁻² ; (M)_(n) '[OsNX₅ ]⁻² ; and mixtures thereof: wherein X is halogen independently selected from the group consisting of F, Cl, Br and I; n is an integer which can vary from 1 to 6 (e.g. 3 to 5), M is a cation including cations of alkali metals, (e.g., Li, Na, K, Rb, Cs, Fr), alkaline earth metals (e.g., Be, Mg, Ca, Sr, Ba, Ra), ammonium (i.e., NH₄ +), tetrahydrocarbyl ammonium (e.g. (R)₄ N⁺) and tetrahydrocarbyl phosphonium (e.g. (R)₄ P⁺) said tetrahydrocarbyl groups being as defined in connection with Group 5 Co-catalysts III discussed below; and n' is a number which is selected in conjunction with the valence of cation M to achieve a neutral complex; preferably n' is 1.

Representative examples of such compounds include OsF₃, OsCl₃, OsBr₃, OsI₃, OsF₄, OsCl₄, OsBr₄, OsI₄, OsF₅, Os(OH)Cl₃, Os(OH)F₃, OsOF₄, OsOCl₄, OsO₃ F₂, OsONCl₄, K₂ [OsCl₂ Br₂ I₂ [, (NH₄)₂ [OsF₆ ], Ca[OsI₆ ], Li₂ [OsO₂ Cl₄ ], (CH₃ CH₂)₄ N[Os(OH)Cl₅ ], Mg[OsO₄ F₂ ], Na₂ [Os(OH)₂ Cl₂ ], Ba[OsNCl₅ ], K₂ [OsNCl₅ ], (CH₃ CH₂)₄ P[Os(OH)Br₅ ], Mg[OsNBr₅ ], Na₂ [OsO₂ (OH)₂ Cl₂ ], Ba[OsNCl₅ ], K₂ [OsNCl₅ ], K₂ [OsNBr₅ ], and mixtures thereof.

The preferred compounds of this class are those having a boiling point at atmospheric pressure of typically greater than about 130° C., preferably greater than about 150° C., and most preferably greater than about 175° C.

The most preferred compounds are those represented by the structural formula OsX₃ such as OsBr₃.

In selecting the appropriate halogen for the osmium-halide the order of preference in terms of activity is Br, Cl, I and F.

The compounds having the formula Os(X)_(n) can be prepared by the general methods described in "Advanced Inorganic Chemistry" by Cotton and Wilkinson (hereinafter Cotton and Wilinson), p. 909 (4th ed. 1980).

Compounds having the formula OsOX₄ and OsO₃ X₂ can be prepared by the method described in the "J. Inorganic Nuclear Chemistry" by Hepworth and Robinson, Vol. 4, p. 24 (1957).

Compounds having the formula Os(OH)X₃ can be prepared by the method described in "Comprehensive Inorganic Chemistry", Trotman-Dickenson (ed.) vol. 3, p. 1217 (1973).

Compounds having the formula OsONX₄ can be prepared by the method described in "Comprehensive Inorganic Chemistry" described above at vol. 3, p. 1233.

Compounds having the formula (M)_(n) '[OsX₆ ]⁻² can be prepared by the general method described in Cotton and Wilkinson, p. 919.

Compounds having the formula (M)_(n) '[OsO₂ X₄ ]⁻² can be prepared by the general method described in Cotton and Wilkinson, p. 917.

Compounds having the formula M⁺¹ [Os(OH)X₅ ]⁻¹ can be prepared by the general method described in "Z. Anorg. Allgen. Chem" by Krauss and Wilken (hereinafter Krauss and Wilken) vol. 137, p. 349 (1924).

Compounds having the formula (M)_(n) '[OsO₄ X₂ ]⁻² can be prepared by the method described in Krauss and Wilken, vol. 145, p. 151 (1925).

Compounds having the formula (M)_(n) '[OsO₂ (OH)₂ X₂ ]⁻² can be prepared by the method described in Cotton and Wilkinson, p. 914.

Compounds having the formula (M)_(n) '[OsNX₅ ]⁻² can be prepared by the method described in "Inorganic Synthesis", by E. G. Rochow, vol. 6, p. 204 (1960).

The disclosures of all of the above references illustrating the methods of preparation of the aforenoted osmium-halide compounds are herein incorporated by reference.

The osmium carbonyl containing compounds suitable for use herein are described in U.S. patent application Ser. No. 420,137, filed Sept. 20, 1982, the disclosure of which is herein incorporated by reference.

More specifically, the term osmium carbonyl compound is defined herein broadly to also include, in addition to compounds, ionic and neutral complexes of osmium with at least one carbonyl ligand and optionally other ligands such as phosphines, hydride, halide and the like as described hereinafter.

Thus, suitable osmium carbonyl compounds include Os(CO)₅, Os₂ (CO)₉, Os₃ (CO)₁₂, Os₅ (CO)₁₆, Os₆ (CO)₁₈, Os₇ (CO)₂₁, and Os₈ (CO)₂₃.

Osmium carbonyl complexes suitable for use as the osmium carbonyl catalyst include those represented by the formulae: [Os(CO)X'₅ ]⁻², [Os(CO)₂ X'₄ ]⁻², [Os(CO)₃ X'₃ ]⁻¹, [Os(CO)₄ X']⁻², and Os(X")_(a) (CO)_(b) (Y)_(c) (PR'₃)_(d), wherein X' is halogen, preferably bromine, X" is independently selected from hydrogen (i.e. hydride), cyclopentadienyl (CPD), and halogen (preferably bromine), Y is independently selected from NO, NH₃, and N₂, R' is a hydrocarbyl group independently selected from alkyl, typically alkyl of from about 1 to 10, preferably from about 1 to 5, most preferably from about 1 to 3 carbons, aryl, typically aryl of from about 6 to about 14, preferably from about 6 to about 10, most preferably about 6 carbons, alkaryl and aralkyl wherein the alkyl and aryl groups thereof are as defined immediately above, "a" and "c" represent numbers of from 0 to about 3, "b" represents a number of at least 1, "d" represents a number of 2 or 3 and the sum of a, b, c, and d is selected in conjunction with the valence of Os to achieve a neutral complex.

Representative examples of suitable osmium carbonyl complexes include [Os(CO)Cl₅ ]⁻², [Os(CO)I₅ ]⁻², [Os(CO)₂ Br₄ ]⁻², [Os(CO)₂ I₄ ]⁻², [Os(CO)₃ I₃ ]⁻¹, [Os(CO)₃ Cl₃ ]⁻¹ [Os(CO)₄ I]⁻², [Os(CO)₄ Cl]⁻², Os(π-CPD)₂ (CO)(Pφ₃)₂, OsCl₂ (CO)(Pφ₃)₂, Os(CO)₃ (Pφ₃)₂, OsHCl(CO) (Pφ₃)₃, OsI(CO)(NO)(Pφ₃)₂, OsHCl(CO)(PEt₂ φ)₃, OsI₂ (CO)(Pφ₃)₂, OsHI(CO)(Pφ₃)₃, and mixtures thereof; "Et" representing ethyl, "φ" representing phenyl, and π-CPD representing pi-bonded cyclopentadienyl.

The preferred osmium carbonyl compound is Os₃ (CO)₁₂.

The aforenoted osmium carbonyl compounds can be prepared by conventional methods as described in "Inorganic Synthesis", Vol. 13, p. 92 (F. A. Cotton ed. 1972); "Quarterly Reviews", Vol. 24, p. 498 (1970); and "Advanced Inorganic Chemistry", Cotton and Wilkinson, p. 1000 to 1017 (3rd ed. 1972).

Representative osmium oxides include OsO₂, OsO₃, OsO₄, and mixtures thereof. The preferred osmium oxide is OsO₄.

Representative ionic osmium oxide compounds are described in U.S. Pat. No. 4,217,291 the disclosure of which is herein incorporated by reference. These ionic osmium compounds can be represented by the formula:

    M'.sub.x OsO.sub.y                                         (II)

wherein M' is a cation of an alkali or alkaline earth metal, ammonium, or tetraalkyl ammonium, preferably tetraalkyl ammonium in which the alkyl group has from about 1 to about 5 carbons, and x and y are numbers such that 2y-x is the valence of the osmium in any compound defined by this formula. While the preferred ionic osmium compounds of this class are the perosmates (M'₂ OsO₅) other ionic osmium compounds such as M'₂ OsO₄ (known as osmates), M'₂ OsO₃, and M'OsO₂ can also be employed.

Representative of osmium complexes include those which form with ligands of PR'₃ (R' being as described above), amines, nitride, π-bonded cyclopentadienyl (π-CPD), and mixtures thereof.

Illustrative osmium phosphine complexes can be represented by the structural formula:

    Os(X").sub.d (Y).sub.e (PR'.sub.3).sub.f                   (III)

wherein X" is independently selected from hydrogen, (e.g., hydrido) cyclopentadienyl (CPD), and halogen (preferably bromine); Y is independently selected from NO, NH₃, and N₂ ; R' is hydrocarbyl group independently selected from alkyl, typically alkyl of from about 1 to about 10, preferably from about 1 to 5, most preferably from about 1 to 3 carbons, aryl, typically aryl of from about 6 to about 14, preferably from about 6 to about 10, most preferably about 6 carbons, alkaryl and aralkyl wherein the alkyl and aryl groups thereof are as defined immediately above, "d" and "e" are numbers of from 0 to about 3, "f" is a number of 2 to 4 (e.g. 2 to 3) and the sum of d, e, and f is selected in conjunction with the valence of Os to achieve a neutral complex.

Representative examples of suitable osmium phosphine complexes include OsH₂ (N₂)(Pφ₃)₃ ; OsH₂ (Pφ₃)₄ ; OsCl₂ (Pφ₃)₃ ; OsCl₃ (NO)(Pφ₃)₂ ; OsCl(NO)(Pφ₃)₂ ; OsCl₂ (NH₃)(PEt₂ φ)₃ ; Os(π-CPD)₂ (NH₃)(Pφ)₂, and mixtures thereof; "Et" representing ethyl, "φ" representing phenyl, and π-CPD representing pi-bonded cyclopentadienyl.

Illustrative osmium amine complexes include aromatic amine complexes illustrated by [Os(bipy)₃ ]⁺² wherein bipy is 2,2'-bipyridine, and [Os(NH₃)₅ X]⁺² wherein X is halogen, preferably Br.

Illustrative osmium nitride complexes include [OsO₃ N]⁻ ; K[OsO₃ N]; and OsO₃ NC(CH₃)₃.

Illustrative π-CPD complexes include Os(π-CPD)₂.

Methods for preparing the aforedescribed osmium complexes are conventional and are summarized in Cotton and Wilkinson "Advanced Inorganic Chemistry" pages 1000-1017 (3rd ed. 1972).

The osmium containing compounds are employed in amounts effective to catalyze the hydroxylation reaction. Thus while any effective amount of osmium catalyst will suffice, it is contemplated that such effective amounts constitute, when the osmium compound is in unsupported form, a ratio of the moles of osmium in the osmium compound to moles of ethylenic unsaturation to be hydroxylated in contact with said osmium compound of typically from about 1×10⁻¹ :1, to about 1×10⁻¹⁰ :1, preferably from about 1×10⁻² :1 to about 1×10⁻⁶ :1, and most preferably from about 1×10⁻² :1 to about 1×10⁻⁵ :1.

Alternatively, such amounts may be expressed as varying from about 1 to about 10,000, preferably from about 10 to about 5,000, and most preferably from about 50 to about 1,000 ppm, based on the total weight of liquid reaction medium including the weight of olefin and any other additives, solvent, or co-catalysts.

While it has been determined that the hydroxylation reaction is first order in the osmium compound, the high cost of osmium will generally militate against using large amounts of osmium in the reaction system.

III Support

The aforedescribed osmium containing compounds can be employed in supported or unsupported form. The use of supported osmium compounds for hydroxylation catalysts is described in U.S. patent application Ser. No. 397,997 filed July 14, 1982 the disclosure of which is herein incorporated by reference.

Accordingly, the material on which the osmium compound is supported can be inorganic or organic but must be insoluble in the reaction mixture under reaction conditions and be capable of physically and/or chemically adsorbing the osmium compound to the extent that it retains a catalytically effective amount of the osmium compound adsorbed thereon.

The catalyst support, when employed, provides not only a surface for the osmium compound to adhere, but also gives physical strength and stability to the same.

The surface area of the support when employed is not critical and typically can vary from about 0.5 to about 400, preferably from about 1 to about 200, and most preferably from about 30 to about 100 m² /g. A desired form of inorganic support is one which has a rough enough surface to aid in retaining the catalyst adhered thereto during handling and under reaction conditions. The support may vary in size but typically is from about 3 to about 400, preferably from about 5 to about 200, most preferably from about 6 to about 100 mesh in the Tyler Standard screen size. Support particles as large as 1 inch in diameter are satisfactory.

Supports much smaller than 325 to 400 mesh normally cause an undesirable pressure drop in the reactor.

The support material is not necessarily inert, that is, the particular support may cause an increase in the catalyst efficiency by its chemical or physical nature or both, but should not adversely influence the hydroxylation reaction. Moreover, the support may impart catalytic activity to an otherwise catalytically inactive, or substantially inactive, material in the absence of the support such as in the instance of osmium metal.

The amount of osmium compound adsorbed on the support is any amount effective to increase the rate and/or selectivity of the hydroxylation reaction relative to the absence of the osmium compound. Thus, while any effective amount may be adsorbed on the support, such effective amounts typically will be from about 0.01 to about 75, preferably from about 0.05 to about 20, most preferably from about 0.1 to about 10.0%, by weight, based on the combined weight of osmium compound and support.

The amount of supported osmium catalyst employed during hydroxylation will likewise be any amount effective to increase the rate and/or selectivity of the hydroxylation reaction relative to the absence of the supported catalyst. The most convenient way to express the amount of supported osmium catalyst (i.e., osmium compound+support) having the aforedescribed amounts of osmium compound adsorbed thereon is as a ratio of the weight of the supported osmium catalyst in contact with the weight of reaction mixture at any given time during the reaction.

Accordingly, while any effective amount of supported osmium catalyst may be employed, it is contemplated that such effective amounts constitute a ratio of parts by weight of supported catalyst to parts by weight of reaction mixture in contact therewith of typically from about 1:0.8 to about 1:20, preferably from about 1:1 to about 1:10, and most preferably from about 1:1 to about 1:4.

Representative supports include alkaline earth metal oxides including MgO, CaO, BaO, BeO and SrO; Sc₂ O₃ ; Y₂ O₃ ; oxides of the Lanthanide series of elements represented by the formula Ln₂ O₃, wherein Ln represents a lanthanide element (i.e., atomic number 58 to 71); alumina (Al₂ O₃); silica (SiO₂); silica gel; silica-alumina; silicon carbide; titania (TiO₂); titania-silica; carbon; activated carbon; Al₂ O₃.B₂ O₃, SiO₂.B₂ O₃, and mixtures thereof; alkaline earth metal orthosilicates such as Ca₂ SiO₄, Mg₂ SiO₄ ; heteropolyanions such as heteropoly tungstates, heteropoly molybdates (e.g., Na₃ PMO₁₂ O₄₀) and the like; and insoluble halogen salts such as Hg₂ I₂, HgI₂, and PbI₂.

Another class of suitable supports include ionic materials onto which the osmium compound can be adsorbed. Included within the scope of ionic supports are zeolites, and ionic polymeric compounds.

Suitable zeolites which can function as supports in accordance with the present invention are exemplified by crystalline aluminosilicate zeolites, preferably zeolites of the faujasite structure. Typically, such faujasite materials possess a SiO₂ :Al₂ O₃ mole ratio in the range of about 2 to about 8 and characteristically have pore diameters in excess of 6 angstroms, which is appropriate for admission of reactants, and to allow exit of the hydroxylated product. The X- and Y-type zeolites are suitable for use as supports herein, with the X-type being preferred. Type X zeolite has a typical oxide formula: Na₂ O:Al₂ O₃ :2.5 SiO₂ :6H₂ O although the mole ratio of SiO₂ :Al₂ O₃ can typically vary from about 2:1 to about 3:1. Type Y zeolite has a typical oxide formula: Na₂ O:Al₂ O₃ :4SiO₂ :8H₂ O although the mole ratio of SiO₂ :Al₂ O₃ can typically vary from about 3:1 to about 6:1. Type L zeolites, natural faujasite materials and mordenites are examples of other zeolites having appropriate pore size and structure for use as a support herein. In general, zeolites having suitable properties can be utilized, whether obtainable as natural materials or prepared synthetically, and can be obtained from commercial sources or prepared by appropriate laboratory crystallization procedures.

The ionic and porous nature of zeolites permits incorporation of the osmium compound therein by conventional ion exchange and/or impregnation procedures as described hereinafter. Similar considerations also apply with respect to ionic polymer supports.

Polymeric ionic support materials typically are employed in porous solid form such as beads, powders, granules, and the like. Suitable polymeric supports are stable to hydroxylation reaction conditions, and sufficiently adsorptive toward the reaction mixture to achieve good contact therewith with the osmium catalytic sites present therein. Accordingly, the polymer must be sufficiently inert and rugged when in contact with the hydroxylation reaction mixture to be resistant to the reaction mixture and easily separated therefrom; and not be abraded, dissolved, decomposed or converted into a soft pulpy gel difficult to separate from the reaction mixture.

Representative classes of suitable ionic polymer supports include conventional weak and preferably strong, acid (cation) or base (anion) exchange resins. Ion exchange resins typically comprise as a back-bone polymer, a polymer crosslinked with a difunctional monomer, to which is attached functional acid or base groups exchanged with various cations or anions (i.e., counter ions) respectively. Representative of weak-acid cation exchange resins include those based on polymers of acrylic or methacrylic acid esters crosslinked with divinyl benzene (DVB). The ester groups are hydrolyzed to produce the functional acid group.

Representative of strong acid cation exchange resins include sulfonated co-polymers of styrene and DVB. Sulfuric acid, sulfurtrioxide, and chlorosulfonic acids can be used for such sulfonation.

Representative of strong-base anion exchange resins include those based on a styrene-DVB co-polymer having an amine functional group, pendant from the aromatic portion of the co-polymer. The base strength of the resin can be varied by varying the nature of the amine functional group from primary to tertiary. The counter ion, prior to incorporation of the osmium compound, for the acid exchange resin is preferably sodium, and for the base-exchange resin, hydroxyl, although any of the conventional counter ions associated with commercially available ion exchange resins can be employed. Other acid or base functional groups can be incorporated into the pendant aromatic groups of the resin tailored specifically to react, complex with, or facilitate adsorption of, the osmium containing compound.

Furthermore, the functional groups of the base ion exchange resin can be partially or completely exhausted (i.e., exchanged) with halide ions which can perform the function of the halide co-catalysts described herein. In this way, the base ion exchange resin support, supports not only the osmium compound but also the co-catalyst halide species resulting in an insolubilized catalytic and co-catalytic system.

Representative commercial ion-exchange resins include those sold under the following tradenames: DOWEX™ available from Dow Chem. Co.; DUOLITE™ available from Diamond Shamrock; AMBERLITE available from Rohm and Haas Co.; and NALCITE™ available from Nalco Chemical Co.

The osmium compound is adsorbed on the support by any way capable of achieving physical and/or chemical adsorption of the latter by the support. Thus, adsorption methods are used which result in retention of the osmium compound in or on the support, and various materials and procedures have been found suitable for this purpose.

For example, an inorganic non-ionic support, e.g., MgO, can be suspended in a suitable solvent together with the osmium compound, preferably a saturated or supersaturated solution of the osmium compound, at room temperature and stirred for a period of from about 0.1 to about 72, preferably from about 0.5 to about 48, most preferably from about 0.5 to about 24 hours. The suspension is then filtered and the recovered solids rinsed, with a suitable solvent. If the support and osmium compound are both dissolved, the solvent can be evaporated and the solids recovered after adsorption of the osmium compound by the support.

The suspension and/or solution of the support and osmium compound can be heated to elevated temperatures although this is not essential.

Suitable solvents and/or suspending media for the aforedescribed purposes include water, alcohols, ketones, ethers, aliphatic hydrocarbons, aromatic hydrocarbons, halogenated hydrocarbons, carboxylic acids and their derivatives such as amides.

Other adsorption methods include vapor phase deposition, electrodeposition, and sublimation.

When employing ionic supports, which typically possess pores capable of retaining the osmium compound, the adsorption method employed can utilize an ion-exchange procedure which results in valence-bonding of the osmium compound with the support and/or impregnation techniques.

For example, when employing zeolites or acid cation exchange resins, conventional ion exchange procedures can be employed to replace the support counter ion with a cationic osmium compound. Such ion exchange can be effected, for example, with solutions of cationic osmium species as described hereinabove, including osmium salts, such as osmium halides, nitrates, or sulfates. The weight ratio of osmium to support will vary depending on the number of anionic sites available on the support. However, it is preferable to maximize this ratio so that as many as possible anionic sites bond with the ionic osmium compound.

Similar exchange procedures can be employed with base anion exchange resins, with the exception that an anionic osmium compound species as described hereinabove is employed to effect the exchange.

Adsorption methods can also be employed which result in impregnation of the porous ionic support with the osmium compound. Thus, the osmium compound can conveniently be impregnated into the support by utilizing a solution of such osmium compound as a slurrying medium for support particles or as an impregnating medium to be adsorbed into the support. The media for incorporating the osmium compound do not necessarily have to completely dissolve the same and in fact may often contain suspended solids.

The supported osmium catalyst is adaptable for use in the various physical forms which are commonly used in a contact bed, or as a coating material on monolithic structures generally being used in a form to provide high surface area. The supported catalyst, can if desired, be composited with various binders which do not adversely affect the catalyst or the reactions in which the catalyst is to be employed.

Depending on the choice of osmium compound and support, the adsorption will be chemical and/or physical.

For example, osmium carbonyls are believed to react with alkaline earth supports such as MgO to form oxygen bonded clusters. Osmium halides or oxy halides are believed to react with metal oxide supports to form oxygen bonded compounds. Osmium oxides are believed to react with metal oxide supports to form osmium oxyanions. Valence bonding of ionic osmium compounds with ion-exchange resins has already been discussed.

IV Co-catalyst System

(a) Co-catalyst I

Co-catalyst I is a term used to refer to at least one organic or inorganic transition metal, i.e., copper, containing compound. Such copper compound will typically be employed as a salt having an anion and a cation, wherein the anion of said salt includes halide, pseudo halide, carboxylate, aryloate, and aryolate and other anions described hereinafter.

The cation transition metal of said Co-catalyst I salts is copper.

More specifically, the anion of Co-catalyst I includes:

(a) halide ions, in their order of preference as follows: bromide, chloride, iodide, fluoride;

(b) carboxylate anions, typically carboxylate anions represented by the structural formula: ##STR2## wherein R₅ is selected from the group consisting of substituted and unsubstituted: alkyl, typically about C₁ to about C₁₀ alkyl, preferably about C₁ to about C₅ alkyl, and most preferably about C₁ to about C₃ alkyl; cycloalkyl, typically about C₄ to C₂₀ cycloalkyl, preferably about C₅ to C₁₅ cycloalkyl, and most preferably about C₆ to C₁₀ cycloalkyl; and aralkyl, typically aralkyl wherein the aryl group thereof is as defined in connection with Ar of structural formula V below and the alkyl group thereof is as defined immediately above; said R₅ substituents including hydroxyl; halide (i.e., F, Cl, Br, and I); ether groups, typically ether groups represented by the structural formulae --O--R₆, and --R₇ --O--R₆ wherein R₆ and R₇ are independently selected from the group consisting of alkyl, typically about C₁ to about C₁₀ alkyl, preferably about C₁ to about C₅ alkyl and most preferably about C₁ to about C₃ alkyl; and ester groups, typically ester groups, represented by the structural formulae ##STR3## wherein R₈ and R₉ which may be the same or different are as defined in connection with R₆ and R₇ ;

(c) aryloate anions, typically aryloate anions represented by the structural formula: ##STR4## wherein Ar is selected from the group consisting of substituted and unsubstituted: aryl, typically C₆ to about C₁₄ aryl, preferably C₆ to about C₁₀ aryl (e.g., C₆ aryl) and alkaryl, typically alkaryl wherein the alkyl group is as defined above in connection with R₅ being alkyl, and the aryl group thereof is as defined above, and wherein said substitutents on the Ar group are as defined above in connection with R₅ ;

(d) aryolate anions, typically aryolate anions represented by the structural formula: ##STR5## wherein Ar is as described above in connection with structural formula IV, and preferably is aryl; and

(e) pseudo halide anions, defined herein to be selected from the group consisting of SNC⁻, CN⁻, SeCN⁻, TeCN⁻, OCN⁻, and CNO⁻ ; and

(f) anions selected from the group consisting of NO₃ ⁻, R₁₀ S⁻, HS⁻, R₁₀ Se⁻, HSe⁻, HTe⁻, and R₁₀ Te⁻, R₁₀ being alkyl typically about C₁ to about C₁₀ alkyl, preferably C₁ to C₅ alkyl.

In short, the Co-catalyst I, when employed as a salt, can be a single salt, or a mixture of salts and said salts can comprise any of the aforenoted transition metal cations associated with any of the aforenoted group (a)-(f) anions.

Representative examples of Co-catalyst I salts include CuF₂, CuBr₂, CuI₂, CuCl₂, CuI, CuCl, CuBr, CuF, copper acetate, copper naphthoate, copper benzoate, copper propanoate, copper nitrate, copper 4-ethyl benzoate, copper 4-butyl benzoate, copper decanoate, copper hexanoate, copper phthalocyanine, copper 2-(methoxymethyl) acetate, copper 3-(ethoxy)propanoate, copper 4-(propoxy carbonyl)-butanoate, copper 3-(propyl carbonyl oxy)propanoate, copper 2-(methyl carbonyloxy methyl)acetate, copper 4-(ethoxy carbonyl methyl)butanoate, copper 4-(ethoxy methyl) benzoate, copper 3-(propoxy) naphthoate, copper 4-(ethoxy carbonyl) benzoate, copper 2-(hydroxy)acetate, copper 2-chloro propanoate, copper 4-(bromo) benzoate, copper 4-(hydroxy) benzoate, copper phenolate, copper naphtholate, copper 4-chloro phenolate, copper 5-(hydroxy) naphtholate, Cu(CN)₂, Cu(SeCN)₂, Cu(TeCN)₂, Cu(OCN)₂, Cu(CH₃ S)₂, Cu(CH₃ CH₂ S)₂, Cu(HS)₂, Cu(CH₃ --CH₂ --CH₂ --Se)₂, Cu(HSe)₃, Cu(HTe)₂, Cu(CH₃ Te)₂, and mixtures thereof.

The preferred Co-catalyst I salts include copper: bromide, chloride, iodide, nitrate and acetate.

The amount of Co-catalyst I employed in the reaction system is related to the amount of osmium in contact with reaction mixture. Thus, while any amount of Co-catalyst I effective to enhance the rate and/or selectivity of the hydroxylation reaction relative to its absence can be employed, it is contemplated that such effective amounts constitute a mole ratio of osmium to the transition metal of Co-catalyst I in the reaction system in contact with the olefin, of typically from about 1:1000 to about 1:1, preferably from about 1:500 to about 1:5, and most preferably from about 1:50 to about 1:10.

(b) Co-catalyst II

Co-catalyst II is defined herein to be at least one compound capable of improving the rate of the hydroxylation reaction when employed in the presence of the osmium compound catalyst, at least one Co-catalyst I, and oxygen.

Suitable Co-catalyst II is characterized by: (1) the possession of at least one tertiary nitrogen; (2) a heteroaromatic or pseudoheteroaromatic ring structure; (3) the absence of primary or secondary nitrogens in the aforenoted ring structures; (4) appropriate steric configuration of any substituents located on the aforenoted ring structures; (5) the absence of nitrogen atoms, in fused bicyclic or tricyclic heteroaromatic ring structures, having a configuration within said ring structures sufficient to enable a bidentate ligand relationship to exist with the transition metal of co-catalysts; and (6) the absence of a 1,3- or 1,4- positional configuration between any two tertiary nitrogens present in said ring structures.

A heteroaromatic ring system or nucleus is defined herein to be one in which at least one carbon atom that is a member of an aromatic ring of an aromatic compound is replaced with a heteroatom (e.g. nitrogen) and the resulting compound contains the maximum number of conjugated double bonds compatible with the valency restrictions imposed by the heteroatom.

A pseudoheteromatic ring structure or nucleus is defined herein to be a 5 carbon membered ring system wherein at least one of the carbons present therein is replaced with a heteroatom (e.g. nitrogen) and the resulting compound contains the maximum number of conjugated double bonds compatible with the valency restrictions imposed by the heteroatom.

Co-catalyst II is conveniently described with reference to pyridine. For example, pyridine can be represented by the following structural formula: ##STR6## Pyridine performs as an excellent rate promoter of, for example, an osmium catalyzed CuBr₂ co-catalyzed, oxygen based olefin hydroxylation system. It is believed that one of the essential features of the pyridine molecule responsible for the observed promoting effect is a tertiary amine nitrogen group located within and forming a part of an aromatic nucleus. However, it has also been found, that as the hydrogens located at the 2 and 6 positions of the pyridine ring are successively replaced with more bulky substituents, e.g. a methyl group, the promoting effect relative to pyridine is decreased due, it is believed, to steric hinderance about the tertiary nitrogen atom. Thus, it is believed that steric freedom about at least one of tertiary nitrogens of Co-catalyst II is an important consideration in selecting the identity of the co-catalyst.

The requirement of the absence of a primary or secondary nitrogen is best illustrated with reference to imidazole represented by the following structural formula: ##STR7## As shown in the Examples, imidazole is not an effective rate promoter due, it is believed, to the presence of a secondary nitrogen at the number 1 position in the ring. When this nitrogen is converted to a tertiary nitrogen by substitution of a methyl group for the replaceable hydrogen, however, rate enhancement is imparted to the compound. The disadvantageous consequences of the presence of a secondary or primary nitrogen is not entirely understood, but it is believed that such nitrogens may be too basic, impart too great an ability to the Co-catalyst II to coordinate with the transition metal of Co-catalyst I to the extent that it effectively prevents the transition metal from performing its intended function, and/or is too readily oxidized in-situ under reaction conditions.

Regarding the limitations of heteroaromatic fused bicyclic or tricyclic ring structures of Co-catalyst II, it has been found that 4,5-diazaphenanthrene and 1,8-diazanaphthalene are not effective rate promoters. Both of these compounds possess two tertiary nitrogens in a fused bicyclic and tricyclic heteroaromatic ring system, respectively as follows: ##STR8## The particular location of the two nitrogens is believed to be such that each nitrogen pair is capable of collectively interacting with the transition metal of Co-catalyst I as a bidentate ligand, the 1,8-diazanaphthalene configuration permitting the formation of a 4 member ring with a central transition metal ion, and the 4,5-diazaphenanthrene permitting the formation of a 5 membered ring with a central transition metal ion. The functioning of the Co-catalyst II as a bidentate ligand is believed to sufficiently disrupt the interaction of the transition metal with other components in the reaction mixture, that the rate enhancement is lost. Thus, it is believed that while Co-catalyst II must possess the ability, complex to some extent, (e.g. as a monodentate ligand) with the transition metal of Co-catalyst II, the stability of the complex should not be so great (e.g. as in bidentate ligands) that the transition metal is, in practical effect, removed from interaction with the remainder of the components of the reaction mixture. Note that for fused tricyclic heteroaromatic ring systems, it is not considered possible for such compounds to act as tridendate ligands, although, if possible, such an occurrence would also sought to be avoided. In accordance with the above theory, and under the replacement nomenclature system of carbocyclic systems described in "Nomenclature of Organic Compounds" ed. Fletcher, J., Dermer, O., Fox, R., Advances in Chemistry Series 126, pp 49 et.seq. (1974), 1,8-diazanaphthalene, 4,5-diazaphenanthrene, and 1,9-diazaanthracene compounds and their derivatives are considered ineffective co-catalysts.

Regarding the limitation relating to the relationship between any two tertiary nitrogens present in the ring structure, it has been found that in the series of diazabenzene isomers, only 1,2-diazabenzene is an effective, albiet slightly effective, rate promoter while 1,4- and 1,3-diazabenzenes actually inhibit the hydroxylation reaction. The reason for this occurrence is not entirely understood, but has led to the conclusion that such 1,4- and 1,3-relationships between tertiary nitrogens present in a mono-, bi- or tri-cyclic fused heteroaromatic ring system should be avoided. Thus, for example, typically in a bi-cyclic ring system a maximum of 3, preferably 2, most preferably 1, tertiary nitrogen(s) will be present therein. Unsuitable diazanaphthalenes include 1,3-, 1,4-isomers thereof.

In view of the above functional requirements, suitable Co-catalysts II for use in the present invention can be represented by at least one of the structural formulae: ##STR9## wherein in structural formula (XIa): Z₂ to Z₆ represent, independently, a methylidyne group (--CH═), a substituted methylidyne group (.tbd.CR₁₁), or a tertiary nitrogen group (--N═), all within a heteroaromatic nucleus containing nitrogen as the heteroatom therein. The substituent R₁₁ of Z₂ to Z₆ is selected from the group consisting of hydroxy; alkyl, typically about C₁ to C₁₀ alkyl, preferably about C₁ to C₅ alkyl, and most preferably about C₁ to C₃ alkyl; aryl, typically about C₆ to C₁₄ aryl, preferably C₆ to C₁₀ aryl, and most preferably C₆ aryl; aralkyl and alkaryl wherein the alkyl and aryl portions thereof are as described immediately above; either groups or ester groups wherein said ether and ester groups are as described in conjunction with R₅ of structural formula (IV) above, said R₁₁ substituents preferably being inert under reaction conditions. In addition, any two R₁₁ groups located on adjacent carbons of said Z₂ to Z₅ groups of structural formula (XIa) together can constitute part of a monocyclic, or fused bicyclic ring system, which partial ring system is: (a) aromatic, or heteroaromatic in nature said heteroatom being nitrogen and (b) completed by, and fused with, parent structure (XIa) above, through said adjacent carbons of the Z₂ to Z₅ groups. Moreover, the replaceable hydrogens of the multicyclic ring system incorporating any two of said R₁₁ groups together, can be substituted with hydroxy, alkyl, aryl, aralkyl and alkaryl groups as defined above.

In structural formula (XIb), Z₇ to Z₉ independently represent a methylidyne group (--CH═), or a substituted methylidyne group (.tbd.CR'₁₁) wherein R'₁₁ is independently selected from the group consisting of alkyl, aryl, aralkyl, and alkaryl as described in conjunction with R₁₁. The substituent R₁₂ of formula (XIb) is selected from the group consisting of alkyl, aryl, aralkyl, and alkaryl as described in conjunction with R₁₁ of formula (XIa), preferably C₁ to C₅ alkyl.

Furthermore as discussed above, in order to impart a rate promoting effect to the Co-catalysts II described by formula (XIa), said formula is also functionally limited by the proviso that in any cyclic ring system defined thereby which contains more than one tertiary nitrogen, the relative configuration between any of said nitrogens within said cyclic ring system: (i) excludes a 1,3- and 1,4-positional relationship; and (ii) prevents Co-catalyst II from acting, under reaction conditions, as a bidentate ligand in conjunction with Co-catalyst I.

Preferably at least one, most preferably both, of said Z₂ and Z₆ groups of formula (XIa) are methylidyne. Likewise, preferably at least one, most preferably both, of said Z₇ and Z₈ groups of formula (XIb) are methylidyne.

Representative compounds suitable for use as Co-catalyst II are provided at Table 1 herein. The most preferred Co-catalyst II is pyridine. ##STR10##

The amount of Co-catalyst II employed in the reaction system will affect the performance thereof. While any amount effective to increase the rate of the hydroxylation reaction can be employed such amounts will generally constitute a ratio of moles of Co-catalyst II to the moles of the transition metal employed as Co-catalyst I of typically from about 1:1 to about 15:1, preferably from about 2:1 to about 10:1, and most preferably from about 3:1 to about 8:1.

If too much Co-catalyst II is employed (e.g. solvent amounts) in the reaction mixture, no effect on reaction rate is observed relative to its absence. Thus, it is not contemplated to employ Co-catalyst II as solvent for the reaction system, if one seeks a rate promoting effect attributable thereto.

Accordingly, the reaction mixture will comprise typically less than 50%, preferably less than 15%, and most preferably less than 5%, by weight of Co-catalyst II, based on the total weight of the liquid contents of the reaction mixture.

(c) Co-catalyst III

Co-catalyst III is a term used herein to describe at least one material, typically employed in an organic or inorganic salt form, which functions in conjunction with Co-catalysts I and II to further improve the rate and/or selectivity of hydroxylation reaction. The use of Co-catalyst III is optional although preferred, particularly with respect to a halide containing Co-catalyst III.

Suitable promoters or Co-catalysts III include alkali (e.g., Li, Na, K, Rb, Cs, and Fr), and alkaline earth metal (e.g., Be, Mg, Ca, Sr, Ba, and Ra): halides, oxides and/or hydroxides, carboxylates, aryloates, aryolates and pseudo halides; tetra hydrocarbyl ammonium: hydroxides, halides, carboxylates, aryloates, and aryolates; tetra hydrocarbyl phosphonium: hydroxides, halides, carboxylates, aryloates, aryolates; hydrogen halides; halogenated hydrocarbons such as alkyl, aryl, aralkyl, alkaryl and cycloalkyl halides; Group III-b (i.e., B, AL, Ga, In, Tl), IV-b (i.e. Si, Ge, Sn, Pb), V-b (i.e., N, P, As, Sb, Bi) and VI-b (i.e., S, Se, Te, Po) halides; and the halogens F₂, Cl₂, I₂, Br₂.

More specifically, suitable alkali and alkaline earth metal halide Co-catalysts III (referred to herein as Group I Co-catalysts III) include the Li, Na, K, Rb, and Cs bromides, iodides, chlorides and fluorides; and Mg, Ca, Sr, and Ba, bromides, iodides, chlorides, and fluorides and mixtures thereof. Preferred Group 1 co-catalysts include the Na, K, Rb, Cs, Mg and Ca halides, particularly bromides.

Suitable alkali and alkaline earth metal hydroxide or oxide co-catalysts (referred to herein as Group 2 co-catalysts III) include LiOH, NaOH, KOH, RbOH, CsOH, Ca(OH)₂, Ba(OH)₂, Mg(OH)₂, the corresponding oxides thereof, and mixtures thereof.

Preferred Group 2 Co-catalysts III include the Na, K, Rb, Mg and Ca hydroxides.

Suitable alkali and alkaline earth metal: carboxylate, aryloate, and aryolate co-catalysts (referred to herein as Group 3 Co-catalysts III) include those which possess as anions respectively:

(a) carboxylate anions represented by the structural formula: ##STR11## wherein R'₁₂ can be substituted or unsubstituted: alkyl, typically alkyl of from about 1 to about 10 carbons, preferably about 1 to about 5 carbons, and most preferably about 1 to about 3 carbons, cycloalkyl, typically cycloalkyl of from about 4 to about 20, preferably from about 5 to about 15, and most preferably from about 6 to about 10 carbons, or aralkyl, typically aralkyl wherein the aryl group thereof is as defined in connection with Ar'-- of structural formula (XIII) below and the alkyl group thereof is as defined immediately above; said R'₁₂ substituents including: hydroxy; halide (i.e., F, Cl, Br, and I); ether groups represented by the structural formulae --O--R₆ and --R₇ --O--R₆ wherein R₆ and R₇ are independently as described in connection with formula (IV) above; and ester groups represented by the structural formulae: ##STR12## wherein R₈ and R₉ which may be the same or different are as defined in connection with formula (IV) above and mixtures thereof.

(b) aryloate anions represented by the structural formula: ##STR13## wherein Ar' is selected from the group consisting of substituted and unsubstituted: aryl, typically aryl of from about 6 to about 14 carbons, preferably from about 6 to about 10 carbons, (e.g., 6 carbons), and alkaryl, typically alkaryl wherein the alkyl group is from about 1 to about 6 carbons, preferably from about 1 to about 3 carbons, and the aryl group thereof is as defined immediately above, and wherein said substituents on the Ar' group are as defined above in connection with R'₁₂ ; and

(c) aryolate anions represented by the structural formula: ##STR14## wherein Ar' is as described above in connection with structural formula (XIII) and preferably is aryl.

Illustrative examples of such Group 3 Co-catalysts III include: sodium acetate, potassium acetate, calcium acetate, cesium acetate, magnesium acetate, potassium ethanoate, sodium propanoate, magnesium butanoate, strontium pentanoate, sodium benzoate, potassium benzoate, magnesium benzoate, calcium benzoate, sodium naphthoate, potassium naphthoate, beryllium naphthoate, sodium 4-(6-methyl-2-naphthyl)-pentanoate, potassium 3-(7-methyl-1-naphthyl)-propanoate, magnesium 2-(4-propyl-1-benzyl)-ethanoate, calcium phenolate, sodium naphtholate, potassium naphtholate, sodium 3-(ethoxy)-propanoate, potassium 4-(propoxycarbonyl) butanoate, calcium 3-(propylcarbonyloxy)-propanoate, magnesium 2-(methylcarbonyloxymethyl)-acetate, beryllium 4-(ethoxy-carbonylmethyl)-butanoate, cesium 4-(ethoxymethyl)-benzoate, sodium 3-(propoxy)-naphthoate, potassium 4-(ethoxy carbonyl)-benzoate, barium 2-(hydroxy)-acetate, rubidium 2-chloropropanoate, magnesium 4-bromobenzoate, magnesium phenolate, and mixtures thereof.

Preferred Group 3 Co-catalysts III include the Na, K, Rb and Cs acetates.

Suitable alkali and alkaline earth metal pseudo halide Co-catalysts III (referred to herein as Group 4 Co-catalysts III) include those which possess pseudo halide anions selected from the group consisting of: SCN⁻, SeCN⁻, TeCN⁻, OCN⁻, and CNO⁻, and mixtures thereof.

Illustrative examples of such Group 4 Co-catalysts III include NaSCN, NaSeCN, KSeCN, CsSeCN, NaTeCN, KTeCN, NaOCN, NaCNO, KOCN, KCNO, CsOCN, CsCNO, CsTeCN, Mg(SeCN)₂, Ca(TeCN)₂, Ca(OCN)₂, Ca(CNO)₂ and mixtures thereof.

Preferred Group 4 Co-catalysts III include the Na, K, Rb and Cs thiocyanates.

Tetrahydrocarbyl ammonium or phosphonium salt co-catalysts (referred to herein as Group 5 Co-catalysts III) possess a cation and an anion. The respective cations can be represented by the respective structural formula (R)₄ N⁺ and (R)₄ P⁺ wherein R is a hydrocarbyl group independently selected from the group consisting of substituted and unsubstituted: alkyl, typically alkyl having from about 1 to about 30 carbons, preferably from about 1 to about 20 carbons, and most preferably from about 1 to about 10 (e.g. 1-5) carbons, aryl, preferably aryl having from 6 to 14 carbons, and most preferably from 6 to about 10 carbons, and alkaryl and aralkyl wherein the aryl and alkyl groups thereof are as defined immediately above; said R substituents being as defined in connection with the substituents of R₁₂ described above. Accordingly, the term hydrocarbyl is intended to include both substituted and unsubstituted groups, and mixtures thereof. The anion of the Group 5 Co-catalysts III are selected from the group consisting of hydroxy, halide, pseudo halide, carboxylate, aryloate and aryolate, said pseudo halide, said carboxylate, aryloate, and aryolate anions, being as defined above in connection with the anions of the alkali and alkali metal Co-catalysts III described above.

Illustrative examples of such Group 5 Co-catalysts III include tetramethylammonium bromide, tetraethylphosphonium chloride, tetradecylphosphonium bromide, tetraphenylammonium chloride, tetraphenylphosphonium bromide, dimethyldiethylammonium iodide, methyltriethylphosphonium chloride, tetrabutylammonium chloride, phenyltrimethylammonium bromide, phenyltrimethylphosphonium chloride, phenyltriethylammonium iodide, phenyltriethylphosphonium chloride, tetraethylammonium hydroxide, tetrabutylammonium hydroxide, tetraethylphosphoniumhydroxide, phenyltriethylammonium hydroxide, phenyltrimethylphosphonium hydroxide, tetraethylammoniumacetate, tetrabutylphosphonium acetate, phenyltriethylammonium acetate, phenyltrimethylphosphonium acetate, tetraethylammonium benzoate, phenyltrimethylphosphonium benzoate, phenyltriethylammonium naphthoate, tetraethylammonium phenolate, tetrabutylphosphonium naphtholate, tetra-2-(methoxy)ethylphosphonium chloride, tetra-4-(propoxymethyl)-phenylammonium bromide, di-3-(methoxycarbonyl)-propyldiethylphosphonium iodide, di-4-(ethylcarbonyloxy)-butyl-dimethyl ammonium chloride, tetra-5-(ethoxycarbonylmethyl)pentylphosphonium bromide, tetra-4-hydroxybutylammonium acetate, tetra-3-chloropropylphosphonium acetate, tetramethylammonium thiocyanate, tetraethylphosphonium selenocyanate, tetra-(4-methylphenyl)ammonium chloride, tetra-(3-phenyl-1-propyl)phosphonium bromide.

Preferred Group 5 Co-catalysts III include the unsubstituted tetra lower alkyl (e.g., C₁ to C₅ alkyl) ammonium hydroxides, bromides, iodides, chlorides, fluorides, and acetates.

Suitable hydrogen halides (referred to herein as Group 6 Co-catalysts III) include HF, HCL, HBr, and HI.

Preferred Group 6 Co-catalysts III include HI, HBr, and HCl.

Suitable halogenated hydrocarbons (referred to herein as Group 7 Co-catalysts III) are described in commonly assigned U.S. patent application Ser. No. 399,270, filed July 19, 1982, by R. Austin and R. Michaelson, the disclosure of which is herein incorporated by reference including any halogenated hydrocarbon compound, preferably a halogenated hydrocarbon compound, wherein the hydrocarbyl portion is selected from saturated aliphatic, saturated alicyclic, and aromatic.

More specifically, suitable Group 7 Co-catalysts III can be represented by the structural formula: ##STR15## wherein R₁₃ can be inertly substituted or unsubstituted: alkyl, typically alkyl of from about 1 to about 20, preferably from about 1 to about 10, most preferably from about 1 to about 5 carbons, aryl, typically aryl of from about 6 to about 14, preferably 6 to about 10, most preferably 6 carbons, aralkyl and alkaryl wherein the alkyl and aryl groups thereof are as defined immediately above, cycloalkyl, typically cycloalkyl of from about 4 to about 20, preferably from about 5 to about 15, and most preferably from about 5 to about 10 carbon atoms; X is at least one halogen independently selected from the group consisting of F, Cl, Br, and I, and preferably Br and/or I; n" is a number of from about 1 to about 10, preferably from about 1 to about 8 (e.g., 2 to 6), and most preferably from about 1 to about 6 (e.g., 2 to 4); and said R₁₃ substituents including hydroxy, ether and ester groups, said ether and ester substituents, being as described in connection with R'₁₂ of structural formula (XII). The term "inertly substituted" is defined herein to mean any organic or inorganic substituent which is stable under reaction conditions and does not adversely affect the performance of said co-catalyst, relative to the unsubstituted halogenated organic compound.

Representative examples of suitable Group 7 Co-catalysts III include iodomethane, bromomethane, iodoethane, bromoethane, 1,2-dibromoethane, chloroethane, 1,2-dichloroethane, 1-iodopropane, 1-bromopropane, 1-chloropropane, 2-iodo-1-methylethane, 2-bromo-1-methylethane, 2-chloro-1-methylethane, 1-iodobutane, 2-iodobutane, 2-bromobutane, 1-chlorobutane, 2-methyl-2-iodopropane, 2-methyl-2-bromopropane, 1-iodo-1-methylpropane, 1-bromo-1-methylpropane, 1-chloro-1-methylpropane, 1-iodo-1,1-dimethylethane, 1-chloro-1,1-dimethylethane, 1-chloro-1,1-dimethylethane, benzyliodide, phenyliodomethane, phenylchloromethane, phenylbromomethane, 1,2-dichlorobenzene, 2-bromoethanol, 2-chloroethanol, 2-iodoethanol, 1-phenyl-2-iodoethane, 1-phenyl-4,4-dichlorobutane, 1-(1,2-dichloroethyl)-benzene, 1-(1-chloropropyl)-naphthylene and mixtures thereof.

Preferred Group 7 Co-catalysts include iodomethane, bromoethane, 1-bromobutane, 1-iodobutane, 1-bromo-1,1-dimethylethane, 1-iodo-1,1-dimethylethane, 2-iodobutane, 2-bromobutane, 2-methyl-2-iodopropane, 2-methyl-2-bromopropane, 2-bromoethanol, 2-chloroethanol, 2-iodoethanol, and mixtures thereof.

The most preferred Group 7 Co-catalysts III contains bromide and includes 1-bromobutane, bromomethane, 2-bromobutane, 2-methyl-2-bromopropane, 2-bromoethanol, and mixtures thereof.

Representative examples of suitable Group III-b, IV-b, V-B, and VI-b metal halides (according to the periodic chart of Cotton and Wilkinson "Advanced Inorganic Chemistry" (3rd ed. 1972)) referred to herein as Group 8 Co-catalysts III include halides of Al, Ga, In, Tl, Ge, Sn, Pb, P, Si, As, Sb, Bi, S, Se, Te, and Po.

Specific Group 8 metal halides include AlCl₃, GaBr₃, TlCl₃, SiCl₄, SiBr₄, PI₃, PBr₃, SbF₅, SbBr₃, SbI₃, BiCl₃, BiBr₃, AsI₃, AsBr₃, AsCl₃, SeF₄, SeCl₄, SeBr₄, TeF₄ and mixtures thereof.

Suitable halogen Co-catalysts III (referred to herein as Group 9 Co-catalysts III) include F₂, Cl₂, Br₂, and I₂.

Any of the Co-catalysts III described in each of the aforenoted Group 1 to 9 Co-catalysts III can be employed alone or in conjunction with one or more Co-catalysts III in the same group and/or with one or more of the Co-catalysts III in the remainder of said groups in any amounts effective to increase the rate and/or selectivity of the hydroxylation reaction relative to that observed in their absence.

Accordingly, while any effective amount of Co-catalyst III can be employed, it is contemplated that such effective amounts constitute typically from about 0.1 to about 10,000 mole percent, preferably from about 10 to about 1000 mole percent, and most preferably from about 25 to about 75 mole percent, Co-catalyst III, based on the total number of moles of osmium in the osmium catalyst employed.

When a supported osmium catalyst is employed, it typically will be utilized as a fixed bed through which the reaction mixture containing the Co-catalyst I, II, and III preferably are determined in a supported system based on the volume of reaction mixture in contact with the fixed bed of supported osmium at any given time during the hydroxylation reaction (referred to herein as the "effective volume"), e.g., the aforedescribed mole percents and/or ratio are contained in the effective volume of the reaction mixture.

Illustrative examples of suitable Co-catalyst combinations include CuBr₂ and pyridine; Cu(NO₃)₂, pyridine and NaBr; CuCl₂, pyridine, and NaBr; CuBr₂, pyridine, NaBr; copper acetate, pyridine, and tetraethyl ammonium chloride; CuI₂, pyridine, and KBr; Cu(NO₃)₂, pyridine, and CsBr; CuI, pyridine, and NaBr; and Cu(NO₃)₂, pyridine, and n-butyl bromide.

In the aforedescribed catalyst composition comprising at least three components, namely, a catalytically active osmium compound, Co-catalyst I and Co-catalyst II, the third component, i.e., Co-catalyst II, unexpectedly substantially improves the rate of reaction for hydroxylating olefins with molecular oxygen relative to its absence. Although the exact mechanism and reason for this effect is not fully understood, it is considered that the results speak positively for themselves. However, the following is offered as an explanation of the mechanism for the observed catalytic effect in connection with the use of osmium tetroxide as the catalytically active osmium compound, although such explanation is not intended to be exhaustive of all possible mechanistic details. It is known that osmium tetroxide adds across the olefin double bond of the compound to be hydroxylated to yield an intermediate cis-ester as follows: ##STR16##

The osmium complex is now formally in the +6 oxidation state. The glycol product can be obtained from this complex by a reductive procedure which is commonly used in the well-known stoichiometric procedure wherein the osmium compound acts as the oxidant, or it can be obtained by oxidative hydrolysis in the presence of an oxidant. This latter route is believed to be operating in the present invention.

Considering this system, it is believed that the copper of Co-catalyst I serves to mediate the reoxidation of osmium by oxygen with concurrent hydrolysis of the glycolate, the copper itself being reduced in the process. The Co-catalyst II, e.g. pyridine, is believed in turn to mediate the reoxidation of the copper through some from of complexed intermediate thereof and/or enhance the solubility of Co-catalyst I in the reaction medium and/or assist in the oxidative hydrolysis of the osmium glycolate. Furthermore, the presence of a halo-moiety in the reaction mixture is believed to facilitate rate of hydrolysis of the glycolate intermediate and may also help to mediate the reoxidation of the transition metal. More specifically, by "halo-" is meant to include halogen in the form of organic and inorganic halide salts or complexes, halogenated hydrocabons, hydrogen halides as well as the free halogens themselves. Accordingly, it is preferred to provide a halo-source in the reaction mixture. This is typically achieved through the use of a copper halide as Co-catalyst I. If, however, Co-catalyst I is not employed as a halide salt, it is preferred to introduce a halo-source through an alternative means. This can easily be achieved through the appropriate selection of any halo-containing Co-catalyst III, such as for example those described hereinabove including alkali or alkaline earth metal halides (e.g. Group I Co-catalyst III), tetra hydrocarbyl ammonium or phosphonium halides (e.g., Group 5 Co-catalysts III), hydrogen halides (e.g. Group 6 Co-catalysts III), halogenated hydrocarbons (e.g. Group 7 Co-catalysts III), metal halides (e.g. Group 8 Co-catalysts III) and halogens (Group 9 Co-catalysts III), as well as transition metal halides. The halo-source can also be any of the osmium-halides described in connection with the suitable osmium containing compounds. For economic reasons it may be more desirable to employ an inexpensive halo-source such as NaBr to fulfill the aforedescribed halogen balance rather than use the more expensive osmium halides or transition metal halides for this purpose.

Thus, for optimum performance of the reaction system, it is preferred to establish a balance, in terms of amounts, between osmium in the osmium catalyst, the copper of Co-catalyst I, and halogen in the halo-source present in the reaction mixture. Accordingly, it is contemplated that the mole ratio of Os:copper:halogen in the halo-source, in contact with the olefin to be hydroxylated be controlled to be typically from about 1:1:1 to about 1:100:1000, preferably from about 1:10:100 to about 1:50:500, and most preferably from about 1:15:20 to about 1:40:200. In satisfying this balance any halogen in the halo-source, e.g. the osmium catalyst, or Co-catalysts is taken into consideration.

While the above discussed mechanism relates specifically to the use of OsO₄ as the osmium catalyst, the other osmium containing compounds discussed above will also form cis-ester intermediates which must be hydrolyzed, although these intermediates are not of the same chemical composition. Thus, the Co-catalysts I and II as well as the halo-source are believed to function through similar mechanisms regardless of the form of the osmium compound employed.

Furthermore, in view of the above discussion, it is recommended for best results that the most preferred valence of copper of Co-catalyst I as initially employed be that which represents the highest stable oxidation state thereof, since such metals must be capable of being reduced upon oxidizing the Os⁺⁶. While this is not critical, it avoids the need in some instances to initially oxidize the transition metal in-situ so that it can be reduced.

While the hydroxylation reaction can be conducted in a heterogeneous multiphase system, the preferred mode for conducting the hydroxylation reaction is in a liquid reaction mixture, preferably provided as a homogeneous or substantially homogeneous medium by using an inert organic solvent to dissolve, where possible, whatever components are employed in the catalyst and co-catalyst system and reactants. Partial immiscibility of the solvent with water is acceptable although not preferred. By an inert solvent is meant one which does not undergo oxidation during the course of the reaction.

Suitable inert organic solvents include aliphatic or aromatic alcohols having from 1 to about 10 carbon atoms, preferably tertiary alcohols, aliphatic or aromatic ketones having from 3 to about 10 carbon atoms, aliphatic or alicyclic ethers having from 2 to about 10 carbon atoms, glycols having from 2 to about 10 carbon atoms, N, N-dialkyl amides having from 3 to about 10 carbon atoms, nitriles having from about 2 to about 10 carbons, aliphatic or aromatic sulfoxides having from 2 to about 14 carbon atoms, aliphatic or aromatic sulfones having from 2 to about 14 carbon atoms, and the like. Examples of suitable solvents include methanol, ethanol, propanol, butanol, hexanol, decanol, t-butyl alcohol, t-amyl alcohol, benzyl alcohol, acetone, methylethyl ketone, methylbutyl ketone, acetophenone, ethylene glycol, propylene glycol, diethylene glycol, tetraethylene glycol, dimethyl formamide, diethyl formamide, dimethyl acetamide, dimethyl sulfoxide, diethyl sulfoxide, N,N-butyl sulfoxide, diphenyl sulfoxide, dibenzyl sulfoxide, dimethyl sulfone, diethyl sulfone, tetramethylene sulfone (sulfolane), diphenyl sulfone, acetonitrile, dioxane, tetrahydrofuran, tetrahydropyran, dioxolane, adiponitrile and mixtures thereof.

The preferred solvents include those which are substantially or completely miscible with water such as t-butyl alcohol, methanol, as well as glycols and/or polyols derived from the olefin being hydroxylated.

The most preferred solvents are dipolar and aprotic such as sulfolane, acetonitrile, N,N-dimethyl acetamide, N,N-dimethylformamide, adiponitrile, and dimethyl sulfone.

The inert solvent is preferably employed in amounts sufficient to achieve a homogeneous solution with respect to at least the olefin and catalyst and Co-catalyst system. Typically such amounts can vary from about 0 to about 98%, (e.g., 10 to 90%), preferably from about about 10 to about 90%, and most preferably from about 20 to about 80%, by weight, based on the total weight of the reaction mixture.

Water is provided to, and/or is present in, the initial reaction mixture in at least a stoichiometric molar ratio with the molar amount of ethylenic unsaturation to be hydroxylated in the olefin. Such ratios preferably are also present in the reaction mixture at any given time after start-up. Accordingly, water is provided in the reaction mixture at molar ratios, of water to ethylenic unsaturation to be hydroxylated in the olefin of from about 1:1 to about 100:1, preferably from about 1:1 to about 10:1, and most preferably from about 1:1 to about 2:1. Such molar ratios typically can be achieved by controlling the amount of water in the reaction mixture to be from about 2 to about 90%, preferably from about 5 to about 50%, and most preferably from about 10 to about 30%, by weight, based on the total weight of the reaction mixture. Preferably the amount of water employed is less than that which will cause separation of the reaction mixture into an aqueous phase and organic phase.

The amount of water employed within the aforedescribed ranges is also influenced by the amount of O₂ in the system. Thus, the mole ratio of H₂ O to O₂ dissolved in the reaction mixture is typically controlled to be from about 1:1 to about 30:1, preferably from about 1:1 to about 15:1, and most preferably from about 1:1 to about 6:1.

The pH of the reaction mixture during the hydroxylation reaction need not be rigidly controlled although it will preferably not be allowed to drop below about 4, preferably not below about 6. Likewise, the pH of the reaction mixture preferably will not be allowed to exceed about 12 although the process can still be conducted at a pH below 4 and above about 12. Active pH control is generally not needed since the pH of the reaction mixture will typically autogeneously vary between about 4 and 12, preferably between about 5 and 12, and most preferably between about 5 and 7.

Furthermore, it will be understood that the use of oxygen in accordance with the process of the present invention inherently avoids the peracid route of olefin hydroxylation, and assures the direct hydroxylation of the olefin. It is also preferred to conduct the hydroxylation reaction in the absence of any organic carboxylic acid such as acetic or propionic acid to avoid esterification of the diol product.

The primary oxidant employed in the present invention is molecular oxygen. Such oxygen can be added as a pure oxygen or as part of an oxygen containing gas such as air or some other oxygen containing gas having one or more inert compounds such as CO₂ or N₂ present therein. Generally, the oxygen containing gas is present within, preferably dissolved in, the reaction mixture in amounts sufficient to achieve hydroxylation of the olefin.

Accordingly, the molar ratio of oxygen to olefin ethylenic unsaturation can vary widely but for safety reasons it is preferably maintained outside explosive limits.

For example, when hydroxylating ethylene or propylene, if oxygen is in excess of stoichiometry, the ratio typically will be 98 weight % oxygen or more and 2% or less of the olefin. Preferably, however, the olefin is employed in excess, preferably large excess, of stoichiometry, and the oxygen concentration of the oxidizing gas typically will be about 10 mole % oxygen and about 90 mole % olefin. When oxygen is in excess of stoichiometry, olefin can be added as the reaction proceeds. On the other hand, where the olefin is in excess of stoichiometry, oxygen can be added during the reaction as the oxygen is consumed.

Accordingly, in view of the above, the oxygen containing gas preferably is dissolved in the reaction mixture in an amount sufficient to achieve a molar ratio of ethylenic unsaturation to be hydroxylated in the olefin to oxygen in excess of 1:1, typically up to as high as 100:1; and outside the explosive limits of the reaction mixture. It is to be noted, that when either olefin or O₂ is employed in substantial excess of stoichiometry for safety reasons the conversion in a batch process will necessarily be very low if based on the component present in large excess. This is not a problem in a continuous process since unreacted components are recycled.

The hydroxylation reaction is typically conducted at temperatures of from about 40° to about 250° C., preferably from about 60° to 200° C., and most preferably from about 80° to about 170° C. to achieve high selectivities for the hydroxylated olefin.

At temperatures greater than the aforenoted ranges, the reaction rate increases subtantially but this usually occurs at the expense of a reduction in selectivity. At very low reaction temperatures, e.g., below about 0° C., the reaction rate decreases to a commercially undesirable degree. Accordingly, while the reaction temperature is not critical and can vary over a wide range, one normally would not operate at temperature extremes outside the aforenoted ranges. Furthermore, since it is preferred to conduct the hydroxylation reaction in the liquid phase, the reaction temperature is typically selected in conjunction with the reaction pressure to achieve this goal.

For the production of ethylene glycol, propylene glycol or any glycol derived from any unsaturated gaseous olefin, the latter may be bubbled through the reaction mixture containing the components described herein or it may be introduced under pressure. Likewise with the oxygen containing gas. However, it is preferred that the reaction takes place in the liquid phase. Consequently, sufficient pressure is preferably employed to maintain the gaseous reactants (i.e., olefin and oxygen) in the liquid phase and/or to dissolve the gaseous reactants into the liquid reaction mixture.

Although the magnitude of the pressure is not critical, it determines the amount of the gaseous reactants that are present in the reaction mixture and therefore affects the rate of reaction. Accordingly, the total pressure of the gases in contact with the reaction mixture is typically controlled to be from about 200 to about 2000 psig, preferably from about 300 to about 1500 psig, and most preferably from about 300 to about 700 psig at the aforenoted reaction temperatures. The partial pressure of each reactant gas, i.e., olefin and oxygen, can be controlled to achieve the aforenoted molar ratios. When the reactant olefin gas is ethylene, the partial pressure (at reaction temperatures) thereof is typically controlled to be from about 100 to about 2000 psig, preferably from about 200 to about 1500 psig, and most preferably from about 300 to about 1200 psig; while when propylene is the reactant olefin, the partial pressure (at reaction temperatures) thereof is typically controlled to be from about 100 to about 2000 psig, preferably from about 200 to about 1500 psig, and most preferably from about 300 to about 1000 psig.

When the olefin reactant is a liquid or is dissolved in the reaction mixture under pressure, its concentration in the reaction mixture typically will vary from about 1 to about 90%, preferably from about 20 to about 80%, and most preferably from about 20 to about 60%, by weight, based on the total weight of the reactant mixture.

In carrying out the invention, olefin, water, oxidant, osmium catalyst, co-catalysts, and optional inert solvent are brought into contact in a manner and under conditions sufficient to hydroxylate the olefin, i.e., to directly convert at least one of the ethylenic unsaturations possessed thereby to its corresponding diol.

Accordingly, the hydroxylation reaction can be performed as a batch reaction, as a continuous reaction or as a semi-continuous reaction. In the batch reaction, the osmium catalyst is charged into the reaction vessel as a solution in the inert solvent along with the Co-catalyst I, Co-catalyst II, optional Co-catalyst III, water, and olefin if in liquid form. The reaction vessel is then pressurized with oxygen and olefin if in gaseous form. It may be desirable to heat the liquid reaction mixture to reaction temperature prior to pressurizing with the reactant gases. The reaction is allowed to proceed to the desired degree of completion.

In the continuous process, the components can be introduced into the inlet of an elongated reactor at a rate such that substantially complete reaction will have taken place by the time the reaction mixture reaches the reactor outlet. The reaction can be carried out in a semi-continuous manner by metering the reactant mixture components into a series of two or more tank reactors at the appropriate rate to maintain the reactor liquid level.

Additionally, the process may be run in either of the aforementioned modes by altering the reaction conditions, and/or, the reactant, solvent, catalyst, and co-catalysts concentrations during the course of the reaction. Thus, the process may be run by changing the temperature, pressure, catalyst concentration, oxidant concentration, and/or olefin concentration.

The spent reaction mixture after removal of unreacted olefin is a solution of product glycol, by-products if any, solvent, water, and catalyst system components. The volatile components are distilled out of the reaction mixture into various fractions leaving non-volatile catalyst system components in the still. The product glycol is then separated from the high boiling distillate.

If the hydroxylation reaction is to be conducted using the supported osmium catalyst, this is typically achieved in fixed bed or slurry form. In the fixed bed mode, the liquid reaction mixture, preferably a homogeneous reaction mixture, is prepared comprising oxidant, co-catalysts, water and olefin and the reaction mixture is passed, preferably continuously, through a fixed bed reactor containing the supported catalyst at reaction temperature and at a rate such that substantially complete reaction will have taken place by the time the reaction mixture reaches the reactor outlet. A variety of fixed bed reactors will be found to be useful and multiple tube heat exchanger type of reactors are satisfactory. In the slurry mode, a reaction mixture containing the above-described components and suspended supported osmium catalyst is charged into a reactor vessel along with olefin and the reaction is allowed to proceed to completion. In a continuous slurry mode, the reaction mixture components can be introduced into the inlet of an elongated reactor adapted to retain, e.g., by filtration, the slurried supported catalyst at a rate such that substantially complete reaction will have taken place by the time the reaction mixture reaches the reactor outlet. The slurry mode can also be carried out in a semi-continuous manner by metering the reactant mixture components into a series of two or more tank reactors adapted as described above at the appropriate rate to maintain the reactor liquid level.

The following examples are given as specific illustrations of the claimed invention. It should be understood, however, that the invention is not limited to the specific details set forth in the examples. All parts and percentages in the examples as well as in the remainder of the specification are by weight unless otherwise specified.

Unless otherwise specified, in the following examples, selectivity, yield, and conversion are calculated as follows: ##EQU1##

The following Comparative Example and Examples 1 to 9 are provided to illustrate not only the effect of pyridine (Co-catalyst II) on the reaction rate, but also the effect of varying the amount of pyridine in relation to Co-catalyst I. The rate enhancement is illustrated by conducting several experiments for the same reaction time and observing the amount of glycol product produced as a function of the amount of pyridine employed.

COMPARATIVE EXAMPLE 1

The following Comparative Example omits pyridine therefrom and is intended to act as a blank against which the following examples can be compared.

Two solutions were prepared as follows: A 30 ml mixture of 80% (V/V) sulfolane and 20% (V/V) water was prepared and 0.19 mmoles of OsO₄ were dissolved therein to form Solution 1. To a 50 ml sulfolane/water (4:1 V/V) mixture was added and dissolved 5 mmoles of CuBr₂ to form Solution 2. Solution 1 was then added to a stirred 300 cc autoclave, equipped with a gas dispersing jet followed by Solution 2 with stirring. Thirty grams of propylene were then charged to the reactor. The stirred solution was then heated to 110° C. and 50 mmoles of molecular oxygen charged thereto. A total pressure of 870 psig was recorded. The reaction was allowed to proceed for 20 minutes measured from completion of the O₂ addition during which time a 20 psig pressure drop was observed. The mixture was then quickly cooled and the pressure released. A brown, turbid solution (pH 3.5) was obtained from the reactor and analyzed by gas chromatography (5% SP-100 on Supelcoport) and showed the production of 16 mmoles of propylene glycol. This corresponds to a 16% yield of propylene glycol based on oxygen charged. Minor amounts of acetone 1,2-dibromopropane, and bromopropanol were also produced. The results are summarized at Table 2, Run 1.

EXAMPLES 1 TO 9

Comparative Example 1 was repeated 9 times in 9 separate experiments with the exception that pyridine was added, in successively higher amounts for each experiment, to Solution 1 prior to introduction into the reactor as shown at Table 2, Runs 2 to 9. The results are also summarized at Table 2.

COMPARATIVE EXAMPLE 2

Comparative Example 1 was repeated with the exception that the sulfolane solvent was omitted from Solutions 1 and 2 and replaced with pyridine. Thus, pyridine is the sole solvent. The results are summarized at Table 2, Run 10.

EXAMPLES 9-17

The following Examples 9-17 are provided to illustrate the performance of various pyridine and imidazole derivatives.

Thus, the procedures of Example 3 were repeated using 12.4 mmoles of a different Co-catalyst II for each of Examples 9-17 to hydroxylate propylene. The results as well as the identity of each Co-catalyst II are summarized in Table 3, Runs 11-19.

COMPARATIVE EXAMPLES 3 TO 12

In accordance with the procedure of Example 3, 12.4 mmoles of a different aromatic amine, imidazole, or aliphatic tertiary amine, outside the scope of the Co-catalyst II of the present invention, for each of Comparative Examples 3 to 12, was employed in the hydroxylation of propylene. The results as well as the identity of each amine employed is summarized at Table 4, Runs 20-29.

EXAMPLE 18

The following example illustrates the use of an osmium halide as the osmium catalyst.

Into a 300 ml titanium autoclave was charged OsBr₃ (0.085 g, 0.20 mmole) in 30 ml of sulfolane/H₂ O (4:1 V/V), CuBr₂ (1.34 g, 6.0 mmole) in 50 ml sulfolane/H₂ O (4:1 V/V), and (13 mmole of pyridine). Propylene (37.0 g) was added to the autoclave and the contents warmed to 90° C. Oxygen was added (60 psig from a 300 cc addition vessel) and the mixture stirred for 1.5 hours upon completion of the oxygen addition. The product solution was analyzed by gas chromatography which indicated the production of 53 mmole PG. The selectivity was about 98% and the conversion based on propylene was 6%. The pH at the end of the run was about 4.5.

COMPARATIVE EXAMPLE 13

Example 18 was repeated with the exception that pyridine was omitted from the reaction mixture. After 1.5 hours of reaction time product analysis showed 23.4 mmoles of propylene glycol. The selectivity to propylene glycol was 85% and the conversion based on propylene was 3.3%.

EXAMPLE 19

Into a 300 ml titanium autoclave was charged Os₃ (CO)₁₂ (0.045 g, 0.05 mmole) in 50 g of N,N-dimethylformamide (DMF), CuBr₂ (1.12 g, 5.0 mmole) dissolved in 26 g DMF, 19.0 g of H₂ O, and pyridine (13 mmole). Propylene (30 g) was added to the autoclave and the contents warmed to 110° C. Oxygen was added (60 psig from a 300 cc addition vessel) and the mixture stirred at 110° C. for one hour upon completion of the oxygen addition. Propylene glycol (18 mmole) was produced at a selectivity of 99%. The conversion based on propylene was 2.5%.

COMPARATIVE EXAMPLE 14

Example 19 was repeated with the exception that pyridine was omitted from the reaction mixture. Product analysis after 1 hour of reaction time showed 11 mmoles of propylene glycol, a selectivity to propylene glycol of 98%, and a conversion based on propylene of 1.5%.

EXAMPLE 20

Into a 300 ml titanium autoclave was charged 1 g of 1% Os metal on silica (0.05 mmole Os) as a slurry in 15 g sulfolane, CuBr₂ (5 mmole) dissolved in 61 g of sulfolane, pyridine (13 mmole) and water (19 g). Propylene (30 g) was added to the autoclave and the contents warmed to 110° C. Oxygen (60 psig) was added and the mixture stirred at 110° C. for 1.5 hours. Propylene glycol (7.1 mmole) was produced with a selectivity of about 86%. The conversion based on propylene was 1.0%.

COMPARATIVE EXAMPLE 15

Example 20 was repeated with the exception that pyridine was omitted from the reaction mixture. Product analysis, after 1.5 hours of reaction time, showed 1.4 mmole of propylene glycol, a selectivity to propylene glycol of 50%, and a conversion based on propylene of <1.0%.

EXAMPLE 21

The following runs illustrate the use of pyridine, a non-halide containing copper salt in conjunction with OsO₄ (Run A) or OsBr₃ (Run B), and a halide containing Co-catalyst III.

RUN A

Into a 300 ml titanium autoclave was charged OsO₄ (0.2 mmole) in 20 g of sulfolane/H₂ O (4:1 w/w), Cu(NO₃)₂.3H₂ O (1.21 g, 5.0 mmole), pyridine (13 mmole), and NaBr (10 mmole) in 75.0 g sulfolane/H₂ O (4:1 w/w). Propylene (30 g) and O₂ (60 psig) were introduced as in all previous examples and the reaction mixture was stirred for one hour. Propylene glycol (80 mmole) was produced at better than 99% selectivity. The conversion based on propylene was 11.2%.

RUN B

Run A was repeated with the exception that OsBr₃ (0.086 g, 0.2 mmole) was used as the osmium source. Product analysis, after one hour of reaction time, showed 52 mmole of propylene glycol, a selectivity to propylene glycol of 99%, and a conversion based on propylene of 7.2%.

The difference in conversions between Runs A and B is attributable to the fact that OsBr₃ requires an induction period during which it is believed that osmium is oxidized to a higher oxidation state before it exerts its catalytic effect. Consequently, given a longer reaction time, the conversion of Run B would be similar to Run A.

COMPARATIVE EXAMPLE 16

Example 21 was repeated with the exception that pyridine was omitted from the reaction mixture. Product analysis, after 1 hour of reaction time showed 35 mmoles (Run A) and 24 mmoles (Run B) of propylene glycol, a selectivity to propylene glycol of 98% (Run A) and 96% (Run B), and a conversion based on propylene of 4.9% (Run A) and 3.4% (Run B).

EXAMPLE 22

The following example illustrates the use with pyridine of a non-halide containing copper salt co-catalyst, OsO₄ (Run A'), or OsBr₃ (Run B') in the absence of a halide containing Co-catalyst III.

RUN A'

Example 21 (Run A) was repeated in the absence of NaBr. Product analysis, after one hour of reaction time, showed 20 mmoles of propylene glycol, a selectivity to propylene glycol of greater than 99%, and a conversion based on propylene of 2.8%.

RUN B'

Example 21 (Run B) was repeated in the absence of NaBr. Product analysis, after one hour of reaction time, showed 13.4 mmole of propylene glycol, a selectivity to propylene glycol of greater than 99%, and conversion based on propylene of 1.9%.

COMPARATIVE EXAMPLE 17

Example 22 was repeated with the exception that pyridine was omitted from the reaction mixture. Product analysis, after 1 hour of reaction time, showed 7.4 mmoles (Run A') and 3.3 mmoles (Run B') of propylene glycol, a selectivity to propylene glycol of 88% (Run A'), and 95% (Run B'), and a conversion based on propylene of 1.1% (Run A') and 0.5% (Run B').

COMPARATIVE EXAMPLE 18

Example 18 was repeated with the exception that the Co-catalyst I (the copper salt) was omitted from the reaction mixture. Product analysis after 1 hour reaction time, showed 0 mmoles of propylene glycol, a selectivity to propylene glycol of 0%, and a conversion based on propylene of 0%.

EXAMPLE 23

This example illustrates the use of higher amounts of oxygen than the previous examples, thereby relieving the limitations on conversion imposed by using excess propylene and calculating the conversion based on propylene.

To 20 ml of a mixture of 65 volume % N,N-di-methylformamide (DMF) and 35 volume % water was added 0.19 mmoles of OsO₄ and 12.4 mmoles of pyridine. To 36 ml of a second solution of 65 volume % DMF and 35 volume % water was added 5.0 mmoles of CuBr₂. These solutions were added successively to a 300 cc stirred autoclave equipped with a gas dispersing jet, followed by 30 g of propylene. The mixture was heated to 140° C. with stirring. At 140° C. oxygen was added in decreasing increments every five minutes for a period of one hour. The oxygen level was thus maintained close to, but not exceeding, the upper-explosive limits of the propylene-oxygen mixture. After one hour, oxygen was added at six minute intervals for 42 more minutes. At this point no more oxygen was added and the reaction was allowed to continue for 18 more minutes followed by rapid cooling. A pressure drop of 450 psig was recorded throughout the course of the reaction. A total of about 260 mmoles of O₂ was added, and analysis by gas chromatography showed that 496 mmoles of propylene glycol were produced. Selectivity to propylene glycol was 98.7% with a conversion based on propylene of 70.4%. The yield of propylene glycol was 69.5%.

                                      TABLE 2                                      __________________________________________________________________________      Run. No.                                                                          Ex. or Comp. Ex. No. 1                                                             Pyri- dine (mmoles)                                                                 Pyr/Cu Mole Ratio                                                                   Pressure Drop Observed (psig)                                                       pH of Product Sol.                                                                  Reac. Time (min.)                                                                  ##STR17##    Conv. %                                                                            P.G. Yield (%)                __________________________________________________________________________      1 Comp.                                                                               0    0   20   3.5  20  16     75    3.0 2.23                              Ex.1                                                                         2 1    2.5  0.5  5   3.8  20  19.5   83    3.3 2.73                            3 2    5.0  1.0 25   4.0  20  31.0   100   4.3 4.3                             4 3    12.4                                                                                2.5 55   5.1  20  59.0   100   8.3 8.3                             5 4    19.0                                                                                3.75                                                                               75   5.3  20  61.0   100   8.5 8.5                             6 5    25.2                                                                                5.0 90   5.5  20  69.0   100   9.7 9.7                             7 6    30.2                                                                                6.0 70   5.5  20  57.5   100   8.1 8.1                             8 7    35.3                                                                                7.0 60   5.6  20  48.0   100   6.7 6.7                             9 8    50.4                                                                                10.0                                                                               60   5.7  20  45.0   100   6.3 6.3                            10*                                                                               Comp.                                                                              990  200   5   6.5  20  14.7   100   2.1 2.1                               Ex. 2                                                                       __________________________________________________________________________      P.G. = propylene glycol product                                                Pyr = pyridine                                                                 *This run illustrates use of Pyridine as a solvent                       

                                      TABLE 3                                      __________________________________________________________________________      Run. No.                                                                          Ex. No.                                                                           ##STR18##  pH of Product Sol.(˜)                                                         Reaction Time (min.)                                                                ##STR19##  Conv. (%)                                                                          P.G. Yield (%)                      __________________________________________________________________________     11  9 2,4-DMP                                                                              12.4 5    20   53.0  100  7.4 7.4                                  12 10 3,5-DMP                                                                              12.4 5    20   63.3  100  8.9 8.9                                  13 11 2-MP  12.4 5    20   39.2  100  5.5 5.5                                  14 12 4-MP  12.4 5    20   59.0  100  8.3 8.3                                  15 13 4-PP  12.4 5    20   54.5  100  7.6 7.6                                  16 14 2,6-DMP                                                                              12.4 5    20   20.0  100  2.8 2.8                                  17 15 1,2-DAB                                                                              12.4 5    20   20.0  100  2.8 2.8                                  18 16 1-MIm 12.4 5.0  20   56.5  100  7.9 7.9                                  19 17 1,2-DMIm                                                                             12.4 3.5  20   65.0  100  9.1 9.1                                  __________________________________________________________________________      DAB = diazabenzene                                                             DMP = dimethyl pyridine                                                        MP = methyl pyridine                                                           PP = phenyl pyridine                                                           P.G. = propylene glycol product                                                MIm = methylimidazole                                                          DMIm = dimethylimidazole                                                 

                                      TABLE 4                                      __________________________________________________________________________      Run. No.                                                                          Comp. Ex. No.                                                                      ##STR20##  pH of Product Sol.                                                                  Reaction Time (min.)                                                                ##STR21##  Conv. (%)                                                                          P.G. Yield (%)                     __________________________________________________________________________     20  3  TEA   12.4 7.5  20   9.4   100  1.3 1.3                                 21  4  QNL   12.4 8.6  20   9.7   100  1.4 1.4                                 22  5  2,2'-BIP                                                                             12.4 5.5  20   0     0    0   0                                   23  6  1,4-DAB                                                                              12.4 4.0  20   1     0    0   0                                   24  7  BI    12.4 5.0  20   6     70   1.2 0.8                                 25  8  1,3-DAB                                                                              12.4 4.5  20   6     100  0.8 0.8                                 26  9  TMED  12.4 5.9  20   0     0    0   0                                   27 10  Im    12.4 5.2  20   15.5  100  2.2 2.2                                 28 11  1,8-DAN                                                                              12.4 3.5  20   6.0   100  0.8 0.8                                 29 12  4,5-DAP                                                                              12.4 5.5  20   0     0    0   0                                   __________________________________________________________________________      TEA = Triethylamine                                                            QNL = quinuclidine                                                             BIP = bipyridine.2]octane)                                                     DAB = diazabenzene                                                             BI = benzimidazoline                                                           TMED =                                                                         Im = imidazoleramethylenediamine                                               DAN = diazanaphthalene                                                   

COMPARATIVE EXAMPLE 19

The following Comparative Example illustrates the uniqueness of the interaction of copper with pyridine in the process of the present invention by substituting a different transition metal salt, i.e., manganese acetate (i.e. Mn(OAc)₂) for the copper salt.

RUN A

Accordingly, into a 300 ml titanium autoclave was charged OsBr₃ (0.08 g, 0.4 mmole), Mn(OAc)₂ 4H₂ O (1.22 g, 5.0 mmole), and (C₂ H₅)₄ NOAc (1.31 g, 5.0 mmole) dissolved in 95.6 g of sulfolane:H₂ O 4:1 w/w solution. Propylene (30 g) was then added and the contents warmed to 110° C. Oxygen (60 psig) was then added and the reaction mixture stirred for 2.0 hours from completion of the addition. The reaction mixture was then analyzed for product and found to contain 30.0 mmole of propylene glycol. The selectivity to propylene glycol was 85.0% with a conversion based on propylene of about 4.2%. The pH at the end of the reaction was about 5.3.

RUN B

A run identical to Run A above was carried out except pyridine (1.03 g, 13.0 mmole) was added to the reaction mixture. The product solution was analyzed after two hours from completion of the O₂ addition and found to contain 5.3 mmoles of propylene glycol with a selectivity to the same of about 50%. This corresponds to a propylene conversion of about 1%. The pH at the end of the reaction was about 5.3.

From the results of Runs A and B it can be seen that pyridine actually decreases the selectivity and conversion is conjunction with Mn and therefore its interaction with the reaction mixture components is one of rate inhibition rather than acceleration.

DISCUSSION OF RESULTS

Referring to Table 2, it can be seen that pyridine can increase the rate of reaction by as much as 4 times the rate in its absence. The degree of rate enhancement however is a function of the amount of pyridine employed in relation to the amount of Co-catalyst I employed. This relationship is not linear, however, the rate enhancement increasing to a pyridine:Cu mole ratio of about 5:1 (Run 6) and then decreasing at higher pyridine levels until the use of pyridine as the principal solvent (Run 10) results in oxidation rates no better than in its absence and actually reduces the oxidation rate below that of the blank (Run 1). The reason for this occurrence is not entirely understood, but it is evidence that pyridine is not operating via the same mechanism as when employed as a promoter for stoichiometric oxidations which do not employ a transition metal co-catalyst.

Referring to Table 3, it can be seen that a variety of pyridine or imidazole derivatives are also effective rate promoters. The different degrees of rate enhancement observed for the various pyridine derivatives is believed to be attributable, in part, to the ability of the nitrogen of Co-catalyst II to complex with the transition metal of Co-catalyst I.

Thus, the di-substituted pyridine, 2,6-dimethyl pyridine (Run 16), which has a relatively high degree of steric hindrance about the nitrogen bonding site, was found to be a less effective promoter for propylene hydroxylation than 3,5-dimethylpyridine (Run 12) having no steric hindrance. Furthermore, the 3,5-dimethylpyridine actually exhibited a slightly higher degree of rate enhancement than pyridine itself. Partially hindered 2,4-dimethylpyridine (Run 11) is intermediate in ability to promote hydroxylation. The effect of steric condiserations on rate enhancement is also illustrated by the mono substituted pyridine derivatives of 2- and 4-methylpyridine, the latter showing enhancement equivalent to that of pyridine (Run 14) and the former (Run 13) being partially hindered and only 66% as effective. The aromatic substituted pyridine 4-phenylpyridine (Run 15) was also observed to be an effective promoter. In the imidazole derivative series, it can be seen that 1-methyl imidazole (Run 18) and 1,2-dimethylimidiazole are effective rate enhancers, while imidazole itself (Run 27) has practically no effect.

In the diazabenzene series of promoters, it can be seen that only 1,2-diazabenzene (Run 17) results in a slight rate enhancement, in contrast to 1,3-diazabenzene (Run 25) and 1,4-diazabenzene (Run 23) which actually reduce the reaction rate (e.g. conversion) over similar reaction times.

Thus, from the above observations it can be concluded that the selection of an appropriate Co-catalyst II will be influenced by consideration of the balance between the steric effect an organic substituent will have on the pyridine ring and any desirable rate enhancement chemically induced by the presence of said substituent on the pyridine ring, e.g., through alterations in the electronegative properties of the nitrogen atom.

Referring to Table 4, it can be seen that the mere possession of a tertiary nitrogen by a compound is not indicative of its ability to promote the subject reaction. Thus, triethylamine, (Run 20), N,N,N',N'-tetramethylenediamine (Run 26), 1-8-diazanaphthalene (Run 28), 4,5-diazaphenanthrene (Run 29), 1,3-diazabenzene (Run 25), benzimidazoline (Run 24), quinuclidine (Run 21), 2,2'-bipyridine (Run 22) and 1,4-diazabenzene (Run 23) actually decreased the reaction rates relative to their absence and/or inhibited the reaction completely. Such data are further evidence that the Co-catalysts II described herein operate through a mechanistic route quite different than that observed for tertiary amines in conjunction with conventional tertiary amine promoted stoichiometric osmium oxidations of olefins. For example, not only has pyridine been employed for such stoichiometric oxidations, but also methyl substituted pyridines, 2,2'-bipyridine and quinuclidine. In fact, 2,2'-bipyridine has actually been observed to induce a much greater rate enhancement than pyridine for such sotichiometric oxidations. However, when such materials are employed with transition metal in an osmium catalytic oxidation, the rate of reaction is actually decreased, and in the case of 2,2'-bipyridine, the reaction is practically terminated. Thus, many of the conventional tertiary amine promoters in stoichiometric oxidations become inhibitors in the reaction system of the subject invention.

The principles, preferred embodiments, and modes of operation of the present invention have been described in the foregoing specification. The invention which is intended to be protected herein, however, is not to be construed as limited to the particular forms disclosed, since these are to be regarded as illustrative rather than restrictive. Variations and changes may be made by those skilled in the art without departing from the spirit of the invention. 

What is claimed is:
 1. A process for hydroxylating at least one olefinic compound having at least one ethylenic unsaturation which comprises reacting said olefinic compound in the presence of oxygen, water and a catalyst composition, in a manner and under conditions sufficient to convert catalytically at least one of said ethylenic unsaturation directly to its corresponding diol, said catalyst composition comprising:(a) at least one catalytically active osmium containing compound; (b) at least one transition metal containing Co-catalyst I having an identity and in an amount effective to increase at least one of the rate and selectivity of the hydroxylation reaction relative to its absence, said transition metal being copper; and (c) at least one Co-catalyst II having an identity and in an amount effective to increase the rate of the hydroxylation reaction relative to its absence and represented by at least one of the structural formulae: ##STR22## wherein: (1) in structural formula (XIa):(a) Z₂ to Z₆ independently represent a member selected from the group consisting of a methylidyne group, a substituted methylidyne group represented, by the formula .tbd.CR₁₁, and a tertiary nitrogen group; said R₁₁ substituent being selected from the group consisting of hydroxy, alkyl, aryl, aralkyl and alkaryl; (b) any two of said R₁₁ substituents located on adjacent carbons of said Z₂ to Z₅ groups of structural formula (XIa) together can constitute part of a monocyclic or fused bicyclic ring system, which partial ring systems are (i) aromatic, or heteroaromatic in nature, said heteroatom being nitrogen, and (ii) completed by, and fused with parent structure (XIa) through said adjacent carbons of Z₂ to Z₅ groups; and (2) in structural formula (XIb):(a) Z₇ to Z₉ independently represent a member selected from the group consisting of a methylidyne group, and a substituted methylidyne group represented by the formula .tbd.CR'₁₁ wherein R'₁₁ is independently selected from the group consisting of alkyl, aryl, aralkyl, and alkaryl; and (b) R₁₂ is selected from the group consisting of alkyl, aryl, aralkyl, and alkaryl.
 2. The process of claim 1 wherein the osmium containing compound is selected from the group consisting of osmium oxide, osmium-halide, osmium carbonyl, ionic osmium oxide, and mixtures thereof; Co-catalyst I comprises a transition metal copper salt having a cation and an anion, wherein said anion is of a member independently selected from the group consisting of halide, carboxylate, aryloate, aryolate, pseudo halide, R₁₀ S⁻, HS⁻, R₁₀ Se⁻, HTe⁻, HSe⁻ and R₁₀ Te⁻, R₁₀ being alkyl of from about 1 to about 10 carbons.
 3. The process of claim 2 wherein said catalyst composition additionally comprises at least one halo-source having an identity and in an amount effective to increase at least one of the rate and selectivity of the hydroxylation reaction relative to its absence.
 4. The process of claim 3 wherein said halo-source is selected from the group consisting of halogenated organic hydrocarbon and halide salt wherein the cation of said salt is of a member independently selected from the group consisting of alkali metal, alkaline earth metal, tetrahydrocarbyl ammonium, and tetrahydrocarbyl phosphonium.
 5. The process of claim 1 wherein the olefinic comporund contains from about 2 to about 20 carbons.
 6. The process of claim 1 wherein said Co-catalyst I is a copper halide salt.
 7. The process of claim 1 wherein Co-catalyst II is selected from the group consisting of pyridine, methylpyridine, dimethylpyridine, 4-phenylpyridine, 1,2-diazabenzene, methylimidazole, dimethylimidazole, and mixtures thereof.
 8. The process of any one of claims 3, 4, 6 and 7 wherein the identity and amount of the osmium in the osmium compound, Co-catalyst I, and halo-source, in said catalyst composition, are controlled to achieve in said composition a molar ratio of osmium:transition metal of Co-catalyst I: halogen in the halo-source of from about 1:1:1 to about 1:100:1000.
 9. The process of claim 7 wherein said Co-catalyst II is selected from the group consisting of pyridine, 3,5-dimethylpyridine, 2,4-dimethylpyridine, 2-methylpyridine, 4-methylpyridine, 4-phenylpyridine, 1-methylimidazole, 1,2-dimethylimidazole, and mixtures thereof.
 10. A process for directly hydroxylating olefins which comprises admixing to form a liquid reaction mixture comprising:(1) at least one olefinic compound having at least one ethylenic unsaturation; (2) at least one catalytically active osmium containing compound; (3) at least one transition metal containing Co-catalyst I having an identity and in an amount effective to increase at least one of the rate and selectivity of said hydroxylation reaction relative to its absence, wherein said transition metal is copper; (4) at least one Co-catalyst II having an identity and in an amount effective to increase at least one of the rate and selectivity of the hydroxylation reaction relative to its absence, said Co-catalyst II comprising at least one member selected from the group consisting of pyridine, 3,5-dimethylpyridine, 2,4-dimethylpyridine, 4-methylpyridine, 4-phenylpyridine, 2-methylpyridine, 1-methylimidazole, and 1,2-dimethylimidizole; (5) an oxygen containing gas; and (6) water in at least a stoichiometric molar ratio with the molar amount of ethylenic unsaturation to be hydroxylated in the olefinic compound; said admixing being conducted in a manner and under conditions sufficient to catalytically convert at least one of said ethylenic unsaturation directly to its corresponding diol.
 11. The process of claim 10 wherein said liquid reaction mixture additionally comprises at least one inert organic solvent.
 12. The process of claim 11 wherein said Co-catalyst II comprises less than about 15%, by weight, of said liquid reaction mixture, and said inert organic solvent comprises from about 10 to about 90%, by weight, of said liquid reaction mixture said inert organic solvent being dipolar and aprotic.
 13. The process of claim 10 wherein said Co-catalyst I is a copper halide salt.
 14. The process of claim 10 wherein Co-catalyst II is selected from the group consisting of 3,5-dimethylpyridine, 4-methylpyridine, 4-phenylpyridine, 1-methylimidazole, and 1,2-dimethylimidazole.
 15. The process of claim 10 wherein said osmium compound is at least one osmium oxide.
 16. The process of claim 15 wherein said osmium oxide is OsO₄.
 17. The process of claim 10 wherein said osmium compound is at least one osmium-halide.
 18. The process of claim 17 wherein said osmium-halide is represented by the structural formula OsX₃ wherein X is selected from the group consisting of Br, I, Cl, and mixtures thereof.
 19. The process of claim 18 wherein X is selected from the group consisting of Br and Cl.
 20. The process of claim 10 wherein the osmium compound is at least one osmium carbonyl.
 21. The process of claim 20 wherein said osmium carbonyl is Os₃ (CO)₁₂.
 22. The process of claim 10 wherein said osmium compound is adsorbed on a support.
 23. The process of claim 10 wherein said liquid reaction mixture further comprises a halo-source soluble in said liquid reaction mixture having an identity and in an amount effective to increase at least one of the rate and selectivity of the hydroxylation reaction relative to the absence of said halogen in said halo-source.
 24. The process of claim 23 wherein said halo-source is selected from the group consisting of osmium-halide; copper halide; alkali metal halide; alkaline earth metal halide; tetrahydrocarbyl ammonium halide; tetrahydrocarbylphosphonium halide; halogenated hydrocarbon wherein the hydrocarbyl portion is selected from saturated aliphatic, saturated alicyclic, and aromatic; and mixtures thereof; and wherein in said liquid reaction mixture the mole ratio of osmium:copper:halogen of said halo-source present therein, is from about 1:10:100 to about 1:50:500.
 25. The process of claim 23 wherein said halo-source is selected from the group consisting of copper halide; alkali metal halide; alkaline earth metal halide; tetrahydrocarbyl phosphonium halide; tetrahydrocarbyl ammonium halide; halogenated hydrocarbon wherein the hydrocarbyl portion thereof is selected from saturated aliphatic, saturated alicyclic and aromatic; and mixtures thereof; and wherein said liquid reaction mixture the mole ratio of osmium:copper:halogen present in said halo-source therein, is from about 1:15:20 to about 1:40:200.
 26. The process of any one of claims 10 to 25 wherein said liquid reaction mixture is homogeneous, and wherein in said liquid reaction mixture the osmium compound is present in an amount sufficient to achieve a ratio of moles of osmium in the osmium compound to moles of ethylenic unsaturation to be hydroxylated of from about 1×10⁻² :1 to about 1×10⁻⁶ :1; Co-catalyst I is present in an amount sufficient to achieve a ratio of moles of osmium in the osmium compound to moles of copper in Co-catalyst I of from about 1:500 to about 1:5; and Co-catalyst II is present in an amount sufficient to achieve a ratio of the moles thereof to the moles of copper in the Co-catalyst I of from about 2:1 to about 10:1; water is present in an amount sufficient to achieve a mole ratio of water to ethylenic unsaturation to be hydroxylated of from about 1:1 to about 10:1; and inert organic solvent, when present, is present in an amount of from about 20 to about 80%, by weight, based on the weight of said reaction mixture.
 27. The process of claim 10 wherein said reaction mixture is substantially homogeneous and wherein in said reaction mixture: the osmium containing compound is selected from the group consisting of OsO₄, OsBr₃, OsCl₃, Os₃ (CO)₁₂ and mixtures thereof; the Co-catalyst I is selected from the group consisting of CuBr₂, CuCl₂, and mixtures thereof, and Co-catalyst II comprises less than about 5%, by weight, of the reaction mixture.
 28. The process of claim 27 wherein said olefin is selected from the group consisting of ethylene, propylene and mixtures thereof.
 29. The process of claim 11 wherein the inert organic solvent comprises from about 20 to about 80%, by weight, of the reaction mixture and is selected from the group consisting of sulfolane, acetonitrile, N,N-dimethylacetamide, N,N-dimethylformamide, hydroxylated product and mixtures thereof.
 30. The process of claim 29 wherein Co-catalyst I is CuBr₂ ; Co-catalyst II is pyridine, and the osmium compound is selected from the group consisting of OsO₄, OsBr₃ and mixtures thereof.
 31. The process of claim 10 wherein the hydroxylation reaction temperature is from about 40° to about 250° C., and the reaction pressure is from about 300 to about 1500 psig. 